Methods of controlling ziegler-natta pre-catalyst particles formation and use for olefin polymerization

ABSTRACT

A colloidal suspension includes an organic phase and a complex of Formula I as precursor for Ziegler-Natta catalyst synthesis:
 
XTiCl p (OR 1 ) 4-p .YMg(OR 2 ) q (OR 3 ) t   (I).
 
In Formula I, a molar ratio of X to Y (X/Y) is from 0.2 to 5.0, p is 0 or 1, 0&lt;q&lt;2, 0&lt;t&lt;2, the sum of q and t is 2, R 1 , R 2 , and R 3  are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; and R 2  is not the same as R 3 .

CROSS-REFERENCE TO RELATED APPLICATIONS

This application claims the benefit of and priority to U.S. Provisional Application No. 62/898,207, filed Sep. 10, 2019, the contents of which are incorporated herein by reference in their entirety.

FIELD

The present technology is generally related to polyolefin catalysts. More specifically, the technology is related to Ziegler-Natta catalysts for the preparation of polyolefins.

BACKGROUND

Ziegler catalysts are widely known and used for a variety of polyolefin products. For example, U.S. Pat. No. 4,447,587 describes the preparation of a solid pre-catalyst by dropwise addition of TiCl₄ into a dispersion of magnesium ethylate in diesel oil. The supernatant is washed four times with diesel oil, and the last washing protocol uses diesel oil to obtain the final solid pre-catalyst, which is then activated with triethylaluminum. U.S. Pat. No. 5,648,309 similarly prepares pre-catalysts with the introduction of different transition metals. U.S. Pat. No. 4,972,035 describes the preparation of pre-catalysts from anhydrous magnesium chloride in decane and 2-ethylhexyl alcohol to form a solution, followed by ethyl benzoate addition. The resulting solution is then added dropwise to an excess of TiCl₄, followed by heating. After termination of the reaction, a solid portion was collected through filtration and washed to obtain a granular pre-catalyst having an average particle diameter of 1.0 μm and a particle size distribution that the geometrical standard deviation was 1.2. U.S. Pat. No. 4,933,393 describes the preparation of pre-catalysts by feeding anhydrous magnesium chloride and hexane into a reactor, adding ethanol, diethylaluminum chloride, and TiCl₄. A solid precipitate is then separated by filtering and washed with hexane to obtain the final pre-catalyst as an agglomerate of fine solid particles of about 1 μm in diameter in a plurality of layers.

In other illustrative pre-catalyst preparations, U.S. Pat. No. 6,545,106 describes the preparation of pre-catalysts by preparing magnesium ethylate from magnesium metal with ethanol in the presence of Ti(OBu)₄. In the reaction, the molar ratio of titanium to magnesium is about 2. Following the addition of ethyl benzoate and isobutylaluminum dichloride in hexane, a solid catalytic complex is collected. U.S. Pat. No. 6,174,971 describes the preparation of a pre-catalyst from a slurried mixture of butyl ethyl magnesium, 2-ethylhexanol, and TiCl(OPr^(i))₃ (Pr^(i) is isopropyl) in hexane to obtain a clear solution. The solution may then be treated with triethylaluminum followed by the addition of TiCl₄/Ti(OBu₄) (Bu is n-butyl) to form a precipitate that is then collected. The final pre-catalyst using this recipe includes an extra impregnation step with TiCl₄ and a pre-contact step with triethylaluminum. European Patent No 2 081 969 describes the preparation of pre-catalysts from magnesium powder in chlorobenzene with dibutyl ether, iodine, and butyl chloride, followed by contact with (C₆H₅)SiCl₃ and Si(OCH₂CH₃)₄ to form a suspension. TiCl₄ was then added to the suspension, and a precipitate was collected. U.S. Pat. No. 9,068,025 describes the reaction of a solution of dibutyl magnesium with isooctanol to obtain a clear solution. To the solution is added a solution of polystyrene-polybutadiene triblock copolymer, followed by the addition of BCl₃ and TiCl₄, in sequence, at low temperature. After bringing the temperature to 50° C., a precipitated solid is collected and washed. U.S. Pat. No. 9,587,047 describes the reaction of magnesium ethylate and Ti(OBu)₄ to obtain a clear liquid upon heating. After cooling and dilution with hexane to obtain a clear solution, ethyl aluminum dichloride (EADC) is added, and the mixture refluxed. Upon cooling, a solid is obtained and washed.

SUMMARY

In one aspect a complex of Formula I is provided: XTiCl_(p)(OR¹)_(4-p).YMg(OR²)_(q)(OR³)_(t)  (I). In Formula I, a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; and R² is not the same as R³. In some embodiments, R¹ may be a C₃-C₆ alkyl, R² may be C₂-C₄ alkyl, and R³ may be a C₃-C₆ alkyl. In some embodiments, R¹ may be n-butyl, R² may be ethyl, and R³ may be n-butyl. In any of the above embodiments, p may be 1. In any of the above embodiments, q may be about 1 and t may be about 1. In any of the above embodiments, X may be 0.2 to 0.5 and Y may be 0.6 to 0.8. In any of the above embodiments, the ratio of X:Y may be from 1 to 3. In any of the above embodiments, the ratio of X:Y may be about 2.

In any of the above embodiments, the complex may exhibit a ¹³C NMR spectra having an alkoxide resonance from 50 ppm to 80 ppm versus residual solvent peak of deuterated toluene-d₈. In any of the above embodiments, the complex of may exhibit a ¹³C NMR spectra having an aryloxide resonance from 40 ppm to 120 ppm versus residual solvent peak of deuterated toluene-d₈. In any of the above embodiments, a weight residue obtained by thermal gravimetric analysis (TGA) may be from 20 wt % to 35 wt %. In any of the above embodiments, the complex may exhibit a Fourier Transform Infrared C—H stretching vibration at a wavenumber from 2500 cm⁻¹ to 4000 cm⁻¹.

In another aspect, a colloidal suspension comprising an organic solvent and a complex of Formula I according to any of the above embodiments is provided. According to any embodiments, the organic solvent may include an alkane, aromatic, or a mixture of any two or more thereof. For example, the organic solvent may include n-hexane, n-pentane, cyclohexane, toluene, benzene, benzine, o-cresol, p-cresol, m-cresol, 1,2-dimethylbenzene, 1,3-dimethylbenzene, 1,4-dimethylbenzene, ethylbenzene, cumine, trichloroethylene, trichlorobenzene, o-dichlorobenzene, or a mixture of any two or more thereof.

In any of the above embodiments, the complex exhibits a multimodal domain size of a dispersed phase. In any of the above embodiments, the concentration of the Ti and Mg may be from 1×10⁻⁵M to 2.0 M, as determined by inductively coupled plasma-optical emission spectrometry (ICP-OES). In any of the above embodiments, the multimodal domains may exhibit a first peak with a domain size mean from 1 nm to 10 nm in diameter, and a second peak with a domain size mean from 250 nm to 350 nm in diameter at 20° C. In any of the above embodiments, the multimodal domain size may exhibit a first peak with a domain size mean from 250 nm to 400 nm in diameter, and a second peak with a domain size mean from 4000 nm to 6000 nm in diameter at 50° C. In any of the above embodiments, the multimodal domain size may exhibit a first peak when measured by Focus Beam Reflectance Measurement (FBRM) with a cord length mean from 1 μm to 10 μm, when measured from −30° C. to 60° C.

In yet another aspect, a solid pre-catalyst system is provided that includes solid particles of a composite of a reaction product of a halogenated compound and any embodiment of the complex of Formula I, including the colloidal suspensions of the complex of Formula I, as described herein. In some embodiments, the halogenated compound includes diethyl aluminum chloride (DEAC), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), titanium tetrachloride (TiCl₄), silicon tetrachloride (SiCl₄) or a mixture of any two or more thereof. The halogenated compounds may be in an organic solvent as described above. For example, the halogenated compound may be present in the organic solvent from about 1 to about 80 wt %, from about 5 to about 70 wt %, from about 25 to 70 wt %, or from about 40 to 60 wt %. In some embodiments, the organic solvent may include pentane, hexane, heptane, octane, and the like. In any of the above embodiments, the Ti may be present from 0.5 wt % to 30 wt %, the Mg may be present from 1 wt % to 20 wt %, the Al may be present from 1 wt % to 20 wt %, and/or the solid particles exhibit a D₅₀ from 1 μm to 30 μm. Any of the above embodiments, may further include an alternative Lewis acid compound.

In a further aspect, a method of polymerizing or co-polymerizing an olefin monomer is provided, the method including contacting a reducing agent with a solid pre-catalyst system that includes solid particles of a composite of a reaction product of a halogenated compound and any embodiment of the colloidal suspension of the complex of Formula I as described herein with at least one olefin monomer. In some embodiments, the olefin monomer may include ethylene, propylene, 1-butene, 4-methyl-1-pentene, 1-hexene, 1-octene, or a mixture of any two or more thereof. In any such embodiments, the solid catalyst system may exhibit an activity of greater than 2 kg_(PE)·g_(Cat) ⁻¹h⁻¹. In one embodiment, the olefin may be ethylene, and the method may also include collecting polyethylene exhibiting a viscosity molecular weight (M_(v)) of greater than 1×10⁶ g/mol. In some embodiments, reducing agents include, but are not limited to, diethyl aluminum chloride (DEAC), triethylaluminum (TEA), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), triisobutyl aluminum (TiBA), trimethyl aluminum (TMA), methylaluminoxane (MAO), or a mixture of any two or more thereof.

In a further aspect, a method of polymerizing or co-polymerizing an olefin monomer in presence of a chain transfer agent, such as hydrogen is provided, the method including contacting a reducing agent with a solid pre-catalyst system that includes solid particles of a composite of a reaction product of a halogenated compound and any embodiment of the colloidal suspension of the complex of Formula I as described herein with at least one olefin monomer. In some embodiments, the olefin monomer may include ethylene, propylene, 1-butene, 4-methyl-1-pentene, 1-hexene, 1-octene, or a mixture of any two or more thereof. In any such embodiments, the solid catalyst system may exhibit an activity of greater than 2 kg_(PE)·g_(Cat) ⁻¹h⁻¹. In one embodiment, the olefin may be ethylene, and the method may also include collecting polyethylene exhibiting a number average molecular weight (M_(n)) of greater than 1×10⁴ g/mol, a weight average molecular weight (M_(w)) of greater than 1.5×10⁵ g/mol. The obtained polymers can also be fractionated by crystallization elution fractionation (CEF) technique, which less than 5 wt % of the polymer will be eluted with 1,2-dichloribenzene under 30° C. (X_(Tel<30)° C.^(A)) and more than 90 wt % of the polymer will elute above 90° C. (X_(Tel>85)° C.^(B)). In some embodiments, reducing agents include, but are not limited to, diethyl aluminum chloride (DEAC), triethylaluminum (TEA), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride.

In yet a further aspect, a method of forming a pre-catalyst precursor is provided, the method including contacting a titanium compound of Formula Ti(OR²⁰)₄ with TiCl₄ to form a reactive mixture; adding an alcohol of formula R²⁰OH to the reactive mixture to form a second mixture; adding a magnesium compound of Formula Mg(OR²¹)₂ to the second mixture to form a third mixture having a molar ratio of titanium compound to magnesium compound of 0.2 to 5.0; and heating the third mixture to form a colloidal suspension of the complex of Formula I, as described herein.

In yet a further aspect, a method to prepare a solid pre-catalyst system includes the reaction of the colloidal suspension comprising an organic solvent and a complex of Formula I with a halogenated compound or a mixture of halogenated compounds.

In yet a further aspect, a method to prepare a solid pre-catalyst system includes adding the halogenated compound or a mixture of the halogenated compound into the colloidal suspension comprising an organic solvent and a complex of Formula I under controlled flow rate, temperature, concentration, and/or stirring speed.

In yet a further aspect, a method to prepare a solid pre-catalyst system includes adding the colloidal suspension comprising an organic solvent and a complex of Formula I into the halogenated compound or a mixture of the halogenated compound under controlled flow rate, temperature, concentration, and/or stirring speed.

In yet a further aspect, a method to prepare a solid pre-catalyst system includes adding simultaneously the halogenated compound or a mixture of the halogenated compound and the colloidal suspension comprising an organic solvent and a complex of Formula I into an inert liquid medium under controlled flow rate, temperature, concentration, and/or stirring speed.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a ¹³C NMR spectra of samples of Example 3.

FIG. 2 is the Fourier Transform Infrared (FTIR) spectra of Example 3, Ti(OBu)₄, and Mg(EtO)₂.

FIG. 3 is a graph of the measurement of the unweighted cord length median of a suspension of Example 1 in hexane.

FIG. 4 is a graph of cord length unweighted median under stirring conditions (up to 400 rpm), concentration of [Ti] between 0.076-0.293 mol/L and temperature of 30° C. or 40° C., according to the Example 1.

FIG. 5 is a graph of DLS results for Examples 1-3 samples under the same conditions, and which display a similar bimodal intensity distribution at 25° C.

FIG. 6 is a graph illustrating the effect of reaction temperature on pre-catalyst particle size, according to the Examples.

FIG. 7 is a graph of the concentration of titanium species relative to the Ti—Mg complex consumption and pre-catalyst formation over reaction time assuming immediate conversion of the reactants, according to the Examples.

FIG. 8 is a graph illustrating the effect of Ti—Mg complex concentration on the pre-catalyst particle size, according to the Examples.

FIG. 9 includes illustrations regarding how the terms solution, colloidal solution, suspension, and colloidal suspension are used in the present application.

FIGS. 10A and 10B are illustrations of different reactor setups for formation of the pre-catalysts described herein.

FIG. 11 is a graph of particle size (D₅₀) as a function of stirring rate, according to the examples.

FIGS. 12A and 12B are plots of CE of polymerization performed with catalyst systems prepared in Examples 13 and 14 under different activation conditions, according to the polymerization conditions described in Example 22.

FIG. 13 is a graph of a particle size distribution measured in a Mastersizer 2000 laser diffraction particle size analyzer from Malvern Panalytical, according to the examples.

FIG. 14 includes illustrations of different reactor setups for formation of the pre-catalysts described herein.

FIG. 15 is a graph of particles size peak mode versus temperature for feeding methods B and C.

FIG. 16 is a graph of the turbidity image analysis, according to the Examples.

FIG. 17 is a graph of the turbidity unity that was modeled with respect to time where k_(T)(T) is the TU time constant and is a function of reactor operating temperature, and TU_(max)(T) is the maximum TU for the system, and it is also a function of reactor temperature, according to the Examples.

DETAILED DESCRIPTION

Various embodiments are described hereinafter. It should be noted that the specific embodiments are not intended as an exhaustive description or as a limitation to the broader aspects discussed herein. One aspect described in conjunction with a particular embodiment is not necessarily limited to that embodiment and may be practiced with any other embodiment(s).

As used herein, “about” will be understood by persons of ordinary skill in the art and will vary to some extent depending upon the context in which it is used. If there are uses of the term which are not clear to persons of ordinary skill in the art, given the context in which it is used, “about” will mean up to plus or minus 10% of the particular term.

The use of the terms “a” and “an” and “the” and similar referents in the context of describing the elements (especially in the context of the following claims) are to be construed to cover both the singular and the plural, unless otherwise indicated herein or clearly contradicted by context. Recitation of ranges of values herein are merely intended to serve as a shorthand method of referring individually to each separate value falling within the range, unless otherwise indicated herein, and each separate value is incorporated into the specification as if it were individually recited herein. All methods described herein may be performed in any suitable order unless otherwise indicated herein or otherwise clearly contradicted by context. The use of any and all examples, or exemplary language (e.g., “such as”) provided herein, is intended merely to better illuminate the embodiments and does not pose a limitation on the scope of the claims unless otherwise stated. No language in the specification should be construed as indicating any non-claimed element as essential.

As used herein, the term “solution” refers to a liquid or solid phase containing more than one substance, when for convenience one (or more) substance, which is called the solvent, is treated differently from the other substances, which are called solutes. In such mixture the solute is stabilized by the solvent or simply solvated, as a result the solute may be present in a particle size of 1 nm, or less, in the largest dimension.

As used herein, the term “colloidal solution” refers to a system in which a substance or a mixture of substances form particles or domains which are regularly dispersed in a continuous phase of a different composition. In such system, the particles or domains have a size of from 1 nm to 100 nm in the largest dimension.

As used herein, the term “suspension” refers to a system in which a substance or a mixture of substances form particles or domains while dispersed in a continuous phase of a different composition (or state) having a size of greater than 100 nm in the largest dimension. At this size level aggregation of the individual particles of the material may start to form and precipitate out as sediment without the presence of any means of agitation. The particles or domains may or may not aggregate and disperse regularly in the continuous phase to form a colloidal suspension which does not precipitate or sediment without the presence of any means of agitation. Colloidal suspensions may have domains or particle sizes of from greater than 100 nm to 10 μm. Solutions, colloidal solutions, and suspensions are illustrated in FIG. 9.

In general, “substituted” refers to an alkyl, alkenyl, aryl, or ether group, as defined below (e.g., an alkyl group) in which one or more bonds to a hydrogen atom contained therein are replaced by a bond to non-hydrogen or non-carbon atoms. Substituted groups also include groups in which one or more bonds to a carbon(s) or hydrogen(s) atom are replaced by one or more bonds, including double or triple bonds, to a heteroatom. Thus, a substituted group will be substituted with one or more substituents, unless otherwise specified. In some embodiments, a substituted group is substituted with 1, 2, 3, 4, 5, or 6 substituents. Examples of substituent groups include: halogens (i.e., F, Cl, Br, and I); hydroxyls; alkoxy, alkenoxy, alkynoxy, aryloxy, aralkyloxy, heterocyclyloxy, and heterocyclylalkoxy groups; carbonyls (oxo); carboxyls; esters; urethanes; oximes; hydroxylamines; alkoxyamines; aralkoxyamines; thiols; sulfides; sulfoxides; sulfones; sulfonyls; sulfonamides; amines; N-oxides; hydrazines; hydrazides; hydrazones; azides; amides; ureas; amidines; guanidines; enamines; imides; isocyanates; isothiocyanates; cyanates; thiocyanates; imines; nitro groups; nitriles (i.e., CN); and the like.

The definition of further substituted is expanded to also include alkylation or arylation of the underlying alkyl, aryl, heteroaryl, heterocyclyl, or cyclyl groups. This means that, e.g. an aryl group may also include alkyl groups, aryl groups, fused ring structures, and the like. This also means that general reference to the aryl group, e.g. “phenyl,” includes tolyl, tert-butyl, di-tert-butyl, bi-phenyl, anthracenyl, and the like.

As used herein, “alkyl” groups include straight chain and branched alkyl groups having from 1 to about 20 carbon atoms, and typically from 1 to 12 carbons or, in some embodiments, from 1 to 8 carbon atoms. Alkyl groups may be substituted or unsubstituted. An alkyl group may be substituted one or more times. An alkyl group may be substituted two or more times. Examples of straight chain alkyl groups include methyl, ethyl, n-propyl, n-butyl, n-pentyl, n-hexyl, n-heptyl, and n-octyl groups. Examples of branched alkyl groups include, but are not limited to, isopropyl, sec-butyl, t-butyl, neopentyl, isopentyl groups, and 1-cyclopentyl-4-methylpentyl. Representative substituted alkyl groups may be substituted one or more times with, for example, amino, thio, hydroxy, cyano, alkoxy, and/or halo groups such as F, Cl, Br, and I groups. As used herein the term haloalkyl is an alkyl group having one or more halo groups. In some embodiments, haloalkyl refers to a per-haloalkyl group. Heteroalkyl groups are alkyl groups containing a heteroatom.

Cycloalkyl groups are cyclic alkyl groups such as, but not limited to, cyclopropyl, cyclobutyl, cyclopentyl, cyclohexyl, cycloheptyl, and cyclooctyl groups. In some embodiments, the cycloalkyl group has 3 to 8 ring members, whereas in other embodiments the number of ring carbon atoms range from 3 to 5, 6, or 7. Cycloalkyl groups may be substituted or unsubstituted. Cycloalkyl groups further include polycyclic cycloalkyl groups such as, but not limited to, norbornyl, adamantyl, bornyl, camphenyl, isocamphenyl, and carenyl groups, and fused rings such as, but not limited to, decalinyl, and the like. Cycloalkyl groups also include rings that may further have straight or branched chain alkyl groups bonded thereto as defined above. Representative substituted cycloalkyl groups may be mono-substituted or substituted more than once, such as, but not limited to: 2,2-; 2,3-; 2,4-; 2,5-; or 2,6-disubstituted cyclohexyl groups or mono-, di-, or tri-substituted norbornyl or cycloheptyl groups, which may be substituted with, for example, alkyl, alkoxy, amino, thio, hydroxy, cyano, and/or halo groups.

Alkenyl groups are straight chain, branched or cyclic alkyl groups having 2 to about 20 carbon atoms, and further including at least one double bond. In some embodiments alkenyl groups have from 1 to 12 carbons, or, typically, from 1 to 8 carbon atoms. Alkenyl groups may be substituted or unsubstituted. Alkenyl groups include, for instance, vinyl, propenyl, 2-butenyl, 3-butenyl, isobutenyl, cyclohexenyl, cyclopentenyl, cyclohexadienyl, butadienyl, pentadienyl, and hexadienyl groups among others. Alkenyl groups may be substituted similarly to alkyl groups. Divalent alkenyl groups, i.e., alkenyl groups with two points of attachment, include, but are not limited to,

CH—CH═CH₂,

C═CH₂, or

C═CHCH₃.

As used herein, “aryl”, or “aromatic,” groups are cyclic aromatic hydrocarbons that do not contain heteroatoms. Aryl groups include monocyclic, bicyclic, and polycyclic ring systems. Thus, aryl groups include, but are not limited to, phenyl, azulenyl, heptalenyl, biphenylenyl, indacenyl, fluorenyl, phenanthrenyl, triphenylenyl, pyrenyl, naphthacenyl, chrysenyl, biphenyl, anthracenyl, indenyl, indanyl, pentalenyl, and naphthyl groups. An aryl group with one or more alkyl groups may also be referred to as alkaryl groups. In some embodiments, aryl groups contain 6-14 carbons, and in others from 6 to 12 or even 6-10 carbon atoms in the ring portions of the groups. The phrase “aryl groups” includes groups containing fused rings, such as fused aromatic-aliphatic ring systems (e.g., indanyl, tetrahydronaphthyl, and the like). Aryl groups may be substituted or unsubstituted.

Heterocyclyl or heterocycle refers to both aromatic and nonaromatic ring compounds including monocyclic, bicyclic, and polycyclic ring compounds containing 3 or more ring members of which one or more is a heteroatom such as, but not limited to, N, O, and S. Examples of heterocyclyl groups include, but are not limited to: unsaturated 3 to 8 membered rings containing 1 to 4 nitrogen atoms such as, but not limited to pyrrolyl, pyrrolinyl, imidazolyl, pyrazolyl, pyridinyl, dihydropyridinyl, pyrimidinyl, pyrazinyl, pyridazinyl, triazolyl (e.g. 4H-1,2,4-triazolyl, 1H-1,2,3-triazolyl, 2H-1,2,3-triazolyl etc.), tetrazolyl, (e.g. 1H-tetrazolyl, 2H tetrazolyl, etc.); saturated 3 to 8 membered rings containing 1 to 4 nitrogen atoms such as, but not limited to, pyrrolidinyl, imidazolidinyl, piperidinyl, piperazinyl; condensed unsaturated heterocyclic groups containing 1 to 4 nitrogen atoms such as, but not limited to, indolyl, isoindolyl, indolinyl, indolizinyl, benzimidazolyl, quinolyl, isoquinolyl, indazolyl, benzotriazolyl; unsaturated 3 to 8 membered rings containing 1 to 2 oxygen atoms and 1 to 3 nitrogen atoms such as, but not limited to, oxazolyl, isoxazolyl, oxadiazolyl (e.g. 1,2,4-oxadiazolyl, 1,3,4-oxadiazolyl, 1,2,5-oxadiazolyl, etc.); saturated 3 to 8 membered rings containing 1 to 2 oxygen atoms and 1 to 3 nitrogen atoms such as, but not limited to, morpholinyl; unsaturated condensed heterocyclic groups containing 1 to 2 oxygen atoms and 1 to 3 nitrogen atoms, for example, benzoxazolyl, benzoxadiazolyl, benzoxazinyl (e.g. 2H-1,4-benzoxazinyl etc.); unsaturated 3 to 8 membered rings containing 1 to 3 sulfur atoms and 1 to 3 nitrogen atoms such as, but not limited to, thiazolyl, isothiazolyl, thiadiazolyl (e.g. 1,2,3-thiadiazolyl, 1,2,4-thiadiazolyl, 1,3,4-thiadiazolyl, 1,2,5-thiadiazolyl, etc.); saturated 3 to 8 membered rings containing 1 to 2 sulfur atoms and 1 to 3 nitrogen atoms such as, but not limited to, thiazolodinyl; saturated and unsaturated 3 to 8 membered rings containing 1 to 2 sulfur atoms such as, but not limited to, thienyl, dihydrodithiinyl, dihydrodithionyl, tetrahydrothiophene, tetrahydrothiopyran; unsaturated condensed heterocyclic rings containing 1 to 2 sulfur atoms and 1 to 3 nitrogen atoms such as, but not limited to, benzothiazolyl, benzothiadiazolyl, benzothiazinyl (e.g. 2H-1,4-benzothiazinyl, etc.), dihydrobenzothiazinyl (e.g. 2H-3,4-dihydrobenzothiazinyl, etc.), unsaturated 3 to 8 membered rings containing oxygen atoms such as, but not limited to furyl; unsaturated condensed heterocyclic rings containing 1 to 2 oxygen atoms such as benzodioxolyl (e.g., 1,3-benzodioxoyl, etc.); unsaturated 3 to 8 membered rings containing an oxygen atom and 1 to 2 sulfur atoms such as, but not limited to, dihydrooxathiinyl; saturated 3 to 8 membered rings containing 1 to 2 oxygen atoms and 1 to 2 sulfur atoms such as 1,4-oxathiane; unsaturated condensed rings containing 1 to 2 sulfur atoms such as benzothienyl, benzodithiinyl; and unsaturated condensed heterocyclic rings containing an oxygen atom and 1 to 2 oxygen atoms such as benzoxathiinyl. Heterocyclyl group also include those described above in which one or more S atoms in the ring is double-bonded to one or two oxygen atoms (sulfoxides and sulfones). For example, heterocyclyl groups include tetrahydrothiophene oxide and tetrahydrothiophene 1,1-dioxide. Typical heterocyclyl groups contain 5 or 6 ring members. Thus, for example, heterocyclyl groups include morpholinyl, piperazinyl, piperidinyl, pyrrolidinyl, imidazolyl, pyrazolyl, 1,2,3-triazolyl, 1,2,4-triazolyl, tetrazolyl, thiophenyl, thiomorpholinyl, thiomorpholinyl in which the S atom of the thiomorpholinyl is bonded to one or more O atoms, pyrrolyl, pyridinyl, homopiperazinyl, oxazolidin-2-onyl, pyrrolidin-2-onyl, oxazolyl, quinuclidinyl, thiazolyl, isoxazolyl, furanyl, dibenzylfuranyl, and tetrahydrofuranyl. Heterocyclyl or heterocycles may be substituted.

Heteroaryl groups are aromatic ring compounds containing 5 or more ring members, of which, one or more is a heteroatom such as, but not limited to, N, O, and S. Heteroaryl groups include, but are not limited to, groups such as pyrrolyl, pyrazolyl, triazolyl, tetrazolyl, oxazolyl, isoxazolyl, thiazolyl, pyridinyl, pyridazinyl, pyrimidinyl, pyrazinyl, thiophenyl, benzothiophenyl, furanyl, benzofuranyl, dibenzofuranyl, indolyl, azaindolyl (pyrrolopyridinyl), indazolyl, benzimidazolyl, imidazopyridinyl (azabenzimidazolyl), pyrazolopyridinyl, triazolopyridinyl, benzotriazolyl, benzoxazolyl, benzothiazolyl, benzothiadiazolyl, imidazopyridinyl, isoxazolopyridinyl, thianaphthyl, purinyl, xanthinyl, adeninyl, guaninyl, quinolinyl, isoquinolinyl, tetrahydroquinolinyl, quinoxalinyl, and quinazolinyl groups. Heteroaryl groups include fused ring compounds in which all rings are aromatic such as indolyl groups and include fused ring compounds in which only one of the rings is aromatic, such as 2,3-dihydro indolyl groups. Although the phrase “heteroaryl groups” includes fused ring compounds, the phrase does not include heteroaryl groups that have other groups bonded to one of the ring members, such as alkyl groups. Rather, heteroaryl groups with such substitution are referred to as “substituted heteroaryl groups.” Representative substituted heteroaryl groups may be substituted one or more times with various substituents such as those listed above.

As used herein, the prefix “halo” refers to a halogen (i.e. F, Cl, Br, or I) being attached to the group being modified by the “halo” prefix. For example, haloaryls are halogenated aryl groups.

Groups described herein having two or more points of attachment (i.e., divalent, trivalent, or polyvalent) within the compound of the present technology are designated by use of the suffix, “ene.” For example, divalent alkyl groups are alkylene groups, divalent aryl groups are arylene groups, divalent heteroaryl groups are divalent heteroarylene groups, and so forth.

It has now been surprisingly found that stable, colloidal suspensions of a Ti—Mg complex of Formula I (XTiCl_(p)(OR¹)_(4-p).YMg(OR²)_(q)(OR³)_(t) (I)) may be formed and used as reactant to the preparation of an efficient Ziegler-Natta catalysts for olefin polymerization reactions. The control in the composition of the Ti—Mg complex enables production of a colloidal suspension with domains and aggregates. Without being bound by theory, the aggregation and breakage of the domains appears to be driven by the surface tension of the liquid droplets, the size of which may be influenced by stirring speed, concentration, temperature, solvent medium, and the chemical composition. Therefore, the control of the dimension of the particles dispersed in the continuous phase, which seems to act as a nucleation domain during the pre-catalyst formation, controls the pre-catalyst particle composition and characteristics. Provided herein are the compositions, methods of making the colloidal suspensions, method of making the pre-catalysts from the colloidal suspensions, and methods of using the catalyst system in the preparation of polyolefins.

Furthermore, it has been observed that the particle size of the catalyst system may be controlled by changing the addition order of the reactants. For example, by adding the halogenated compound to a colloidal suspension of a Ti—Mg complex of Formula I, compared to simultaneously adding the colloidal suspension of a Ti—Mg complex of Formula I and the halogenated compound into an inert medium, results in at least a doubling of the D₅₀ particle size of the obtained solid pre-catalyst particles when the stirring rate is the same. Two of the addition methods are exemplified in FIG. 10A and FIG. 10B. Methods of preparation are further described below.

In Formula I, a molar ratio of X:Y is 0.2 to 5.0, p is 0 or 1, 0<q<2, 0<t<2, the sum of q and t is 2, R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; and R² is not the same as R³. In some embodiments, R¹ may be a C₃-C₆ alkyl, R² may be C₂-C₄ alkyl, and R³ may be a C₃-C₆ alkyl. One illustrative and non-limiting embodiment includes where R¹ is n-butyl, R² is ethyl, and R³ is n-butyl. In some embodiments of Formula I, p is 1. In any such embodiments, q may be about 1 and t may be about 1. In some embodiments, X is from 0.2 to 0.5 and Y is from 0.6 to 0.8. The ratio of X:Y may vary, as noted above. For example, the ratio of X:Y may be from 1 to 3, or about 2.

In a carbon-13 nuclear magnetic resonance (¹³C NMR) of the suspended complex of Formula I in hexane and the isolated complex of Formula I, an alkoxide resonance from 50 ppm to 80 ppm versus residual solvent signal of deuterated toluene-d₈ is exhibited (FIG. 1). This is indicative of the mixture of alkoxy groups derived from the Ti—Mg complex. In some embodiments, where the complex of Formula I include an aryloxide group, a ¹³C NMR spectra of the complex may exhibit a resonance from 40 ppm to 120 ppm versus residual solvent signal of deuterated toluene-d₈.

Thermal gravimetric analysis (TGA) may be used to support the characterization of the compounds by comparing actual to theoretical weight loss from a sample of the complex. In the case of the complexes of Formula I, after TGA, the weight residue obtained may be from 20 wt % to 35 wt %.

Like ¹³C NMR and TGA, Fourier Transform Infrared (FTIR) spectroscopy may be used to characterize the complexes. In the compositions of Formula I, the C—H stretch vibration derived from metal-oxygen-C—H may be observed using FTIR at a wavenumber from 2500 cm⁻¹ to 4000 cm⁻¹.

The colloidal suspension of the complex of Formula I may also include an organic phase. For example, the organic phase may be an alkane, aromatic, or a mixture of any two or more thereof. Illustrative examples of the organic phase include, but are not limited to, n-hexane, n-pentane, cyclohexane, toluene, benzene, benzine, o-cresol, p-cresol, m-cresol, 1,2-dimethylbenzene, 1,3-dimethylbenzene, 1,4-dimethylbenzene, ethylbenzene, cumine, trichloroethylene, trichlorobenzene, o-dichlorobenzene, or a mixture of any two or more thereof.

Interestingly, the complexes/colloidal suspensions of the complexes described herein, exhibit a multimodal domain size of a dispersed phase. As used herein a “dispersed phase” is the particles or domains that are of interest which have essentially the properties of a bulk phase of the same composition, while the “continuous” phase is different in composition. In the dispersed phase, the multimodal domain size a first peak with a domain size mean from 1 nm to 10 nm in diameter, and a second peak with a domain size mean from 250 nm to 350 nm in diameter at 20° C. This includes a multimodal domain size exhibiting a first peak with a domain size mean from 250 nm to 400 nm in diameter, and a second peak with a domain size mean from 4000 nm to 6000 nm in diameter at 50° C.

ICP-OES may be used to determine the Ti and Mg concentrations in the compound of Formula I. In some embodiments, the concentration of the Ti and Mg was determined by ICP-OES to be from 1×10⁻⁵M to 2.0 M, as determined by ICP-OES.

One technique for determining the particle size of the complex of Formula I, FBRM. According to FBRM, the complexes and colloidal suspensions may exhibits a first peak with a cord length mean from 1 μm to 10 μm, when measured from −30° C. to 60° C.

In another embodiment, a solid pre-catalyst system is formed from the colloidal suspension of compound of Formula I as described above, and a halogenated compound. In Formula I (XTiCl_(p)(OR¹)_(4-p).YMg(OR²)_(q)(OR³)_(t)), a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; and R² is not the same as R³. The halogenated compound may be a Lewis acid compound. Illustrative Lewis acid compounds may include one or more of diethyl aluminum chloride (DEAC), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), titanium tetrachloride (TiCl₄), and silicon tetrachloride (SiCl₄). In the solid pre-catalyst system, the total amount of Ti may be from about 0.5 wt % to about 30 wt %. In the solid pre-catalyst system, the Mg may be present from about 1 wt % to about 20 wt %. In the solid pre-catalyst system, the Al may be present from about 1 wt % to about 20 wt %. In the solid pre-catalyst system, the solid particles exhibit a D₅₀ from 1 μm to 30 μm if the reaction is carried out with the addition method A (FIG. 10A) and a D₅₀ from 1 μm to 15 μm if the reaction is carried out with the addition method B (FIG. 10B) under similar reaction conditions.

In any of the above embodiments, the solid pre-catalyst system may include a reducing agent. Illustrative reducing agents include, but are not limited to, diethyl aluminum chloride (DEAC), triethylaluminum (TEA), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), triisobutyl aluminum (TiBA), trimethyl aluminum (TMA), methylaluminoxane (MAO), or a mixture of any two or more thereof.

The Ziegler-Natta catalyst systems produced from colloidal suspensions that are described herein may be used as polymerization- or co-polymerization-catalysts for the polymerization of olefins. Accordingly, methods of using any of the pre-catalyst systems produced from the colloidal suspension in a method of polymerization are provided. The methods may include contacting a reducing agent with a solid pre-catalyst system that includes solid particles of a composite of a reaction product of a halogenated compound and a colloidal suspension of complex of Formula I (XTiCl_(p)(OR¹)_(4-p).YMg(OR²)_(q)(OR³)_(t)) as embodied herein with at least one olefin monomer. A wide variety of olefins may be polymerized with the catalysts. Illustrative, non-limiting, olefins may include ethylene, propylene, 1-butene, 4-methyl-1-pentene, 1-hexene, 1-octene, or a mixture of any two or more thereof.

The catalyst efficiency (“CE”) of the solid catalyst systems has been determined to be greater than 2 kg_(PE)·g_(Cat) ⁻¹·h⁻¹. This may include from 2 kg_(PE)·g_(Cat) ⁻¹·h⁻¹ to 50 kg_(PE)·g_(Cat) ¹·h⁻¹, and from 4 kg_(PE)·g_(Cat) ⁻¹·h⁻¹ to 20 kg_(PE)·g_(Cat) ⁻¹·h⁻¹.

In some embodiments of the methods, the olefin may be ethylene, and the polyethylene obtained from the method exhibits an intrinsic viscosity of greater than 1.0 dl/g. This may include from 1 dl/g to 50 dl/g, and from 5 dl/g to 40 dl/g.

In another aspect, methods of forming a pre-catalyst composition that includes the complex of Formula I are provided. The methods include contacting a titanium compound of Formula Ti(OR²⁰)₄ with TiCl₄ to form a reactive mixture. Alcohol of formula R²⁰OH may then be added to the reactive mixture to form a second mixture. To the second mixture is then added a magnesium compound of Formula Mg(OR²¹)₂ to form a third mixture having a molar ratio of titanium compound to magnesium compound of 0.2 to 5.0. Finally, the third mixture is heated to form a complex of Formula I, as described herein, followed by the removal of ethanol as a by-product of this reaction.

In the methods of forming, formation of the reactive mixture may conducted at, or below about ambient temperature to minimize or prevent exothermic runaway. An illustrative temperature is from about 0° C. to 40° C., from about 10° C. to about 40° C., or about 25° C. to about 30° C. Also, the heating of the third mixture is done at a temperature sufficient for the reaction to proceed and to distill the byproduct alcohol from the reaction mixture. While this temperature may vary, it is generally from about 80° C. to about 180° C. In some embodiments, the temperature is from about 100° C. to 160° C.

As an illustrative example of the method of preparation, the reactive mixture is formed by dropwise addition of TiCl₄ to neat Ti(OBu)₄ at a temperature below 30° C. with stirring and in a molar ratio of Ti(OBu)₄/TiCl₄ of about 3. In this case the TiCl₄ acts as chlorinating agent to the Ti(OBu)₄, producing TiCl(OBu)₃ through a radical-interexchange reaction. To this titanium compound, under an inert atmosphere and with stirring, magnesium ethoxide powder is added at molar ratio to the Ti species of 2. The mixture is then heated to 130° C. with stirring until the reaction is complete (from about 4 to 6 hours). In this step, different amounts of butanol are added resulting in a partial or completed exchange reaction with magnesium ethoxide to form magnesium butoxide or a mixture of magnesium ethoxide and butoxide allowing the formation of a clear liquid. The byproduct of this reaction (ethanol) is collected by Dean-Stark trapping. The temperature is then decreased to 100° C. and the complex is suspended in hexane to obtain a colloidal suspension with titanium concentration lower than 0.4 mol/L. During the addition of hexane the temperature is allowed to reach 60° C., where it is maintained with stirring for at least 1 hour. Afterward, the colloidal suspension is stable at room temperature.

In further aspects, the methods of preparing a solid pre-catalyst system as a polyolefin catalyst are dependent upon the reaction conditions and how the colloidal suspension is prepared. For example, in some embodiments, the method of preparing the solid pre-catalyst system includes reacting a colloidal suspension of an organic solvent and a complex of Formula I with a halogenated compound or a mixture of halogenated compounds. In the methods, the complex of Formula I is as described for any embodiment herein. In other embodiments, the method of preparing a solid pre-catalyst system includes adding a halogenated compound or a mixture of the halogenated compound into a colloidal suspension that includes an organic solvent and a complex of Formula I, under controlled flow rate, temperature, concentration, and/or stirring speed. In further embodiments, a method of preparing a solid pre-catalyst system includes adding, simultaneously, a halogenated compound (or a mixture of halogenated compounds) and a colloidal suspension that includes an organic solvent and a complex of Formula I, into an inert liquid medium under controlled flow rate, temperature, concentration, and/or stirring speed.

In the methods, the compound of Formula I, the organic solvents, the colloidal suspensions, the halogenated compound(s), and the pre-catalyst systems are as described above. However, as noted, reaction conditions such as temperature, concentrations, and/or stirring speeds impact the particle size of the domains in the colloidal suspension and the solid pre-catalyst particles. As shown in FIG. 11, increasing the stirring speed from 500 to 1750 rpm decreases the D₅₀ value of the particle size of the pre-catalyst. In some embodiments, the stirring rate in the method is from 50 to 3000 rpm, 200 to 2500 rpm, from 400 to 2000 rpm, or from 500 to 1800 rpm.

Generally, reactive precipitation processes involving chemical reactions lead to a simultaneous and fast occurrence of nucleation, crystal growth and aggregation. Thus, it may be expected that reaction conditions, such as temperature and concentration in addition to the stirring speed, may also influence the mechanisms of particle formation. As illustrated by FIG. 5, the lower is the temperature of the medium the smaller is the domain size in the Ti—Mg complex colloidal suspension, which could suggest better control of the nucleation domains in a reactive precipitation process. It is also known that lower temperature in the reaction medium promotes mechanisms of nucleation and crystal growth, which may result in the formation a smaller pre-catalyst particle sizes, as shown in FIG. 06. On the other hand, as particles are formed, concerns on the increase surface tension in a slurry system should also be taken in account due to the increase of cohesive forces. As shown in FIG. 13, the significant increase of the surface tension at the lowest reaction temperature suggests an important contribution from the aggregation mechanisms that broadens the particle size distribution. The contrary was observed for diluted reaction mediums due to the suppression of cohesive forces throughout the particle formation.

In the above methods, the organic solvent and/or inert liquid medium may individually include, but is not limited to, an alkane, aromatic, or a mixture of any two or more thereof. Illustrative organic solvent and/or inert liquid medium may individually include n-hexane, n-pentane, cyclohexane, toluene, benzene, benzine, o-cresol, p-cresol, m-cresol, 1,2-dimethylbenzene, 1,3-dimethylbenzene, 1,4-dimethylbenzene, ethylbenzene, cumine, trichloroethylene, trichlorobenzene, o-dichlorobenzene, or a mixture of any two or more thereof.

In the methods, the halogenated compound(s) may include, but is not limited to, diethyl aluminum chloride (DEAC), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), titanium tetrachloride (TiCl₄), silicon tetrachloride (SiCl₄) or a mixture of any two or more thereof. In the methods, the halogenated compounds may be diluted in an organic solvent, such as those listed herein, in any embodiment. The concentration of the halogenated compound at addition may be in excess of about 5 wt %.

In the above methods, a concentration of the Ti and Mg in the colloidal suspension is from about 1×10⁻⁵M to about 2.0 M, as determined by ICP-OES.

In any of the embodiments herein, the methods may be conducted at a temperature from about −40° C. to +60° C. In any of the embodiments herein, the methods include a simultaneously feed of the halogenated compound and the colloidal suspension of a complex of Formula I at constant chloride to —OR^(x) molar ratio, where x merely indicates the R¹, R², and R³ groups collectively. In some embodiments the chloride to —OR^(x) molar ratio is from about 0.1 to about 10.

In any of the embodiments herein, the resulting solid pre-catalyst from the method exhibits a Ti content from 0.5 wt % to 30 wt %, a Mg content from 1 wt % to 20 wt %, and/or an Al content from 1 wt % to 20 wt %. The solid pre-catalyst particles obtained from the method may exhibit a D₅₀ from about 1 μm to about 15 μm.

In any of the embodiments herein, the method may further include contacting the solid pre-catalyst system with a reducing agent. Illustrative reducing agents include, but are not limited to, diethyl aluminum chloride (DEAC), triethyl aluminum (TEA), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), triisobutyl aluminum (TiBA), trimethyl aluminum (TMA), methylaluminoxane (MAO), or a mixture of any two or more thereof. In some embodiments, the solid pre-catalyst system may be further contacted with a reducing agent resulting in a solid catalyst system.

The present invention, thus generally described, will be understood more readily by reference to the following examples, which are provided by way of illustration and are not intended to be limiting of the present invention.

EXAMPLES Example 1

Preparation of a colloidal suspension. Step 1: Ti(OBu)₄ (89.1 mL; 0.27 mol) was introduced to a 3 L glass reactor equipped with an overhead stirrer, a Dean-Stark trap, and a reflux condenser under an inert atmosphere at 30° C. The reaction was followed by a dropwise addition of TiCl₄ (9.61 mL; 0.085 mol) while stirring at 250 rpm and maintaining the temperature under 30° C. to form a reactive mixture. Step 2: The reactive mixture was kept under these conditions for one hour, and then anhydrous n-butanol (31.0 mL, 0.34 mol) was introduced at a flow rate of 15 mL/min.¹ Following completion of the n-butanol addition, Mg(OEt)_(2(s)) (77.5 g, 0.68 mol) was slowly added under nitrogen. Step 3: The reaction temperature was raised to 130° C. and the stirring speed to 500 rpm. This condition was maintained for 1.5 hours, followed by the collection of by-products (i.e., ethanol) via the Dean-Stark trap. Additional anhydrous n-butanol (25.0 mL, 0.27 mol) was introduced at a flow rate of 15 mL/min, and the reaction was kept under the same conditions for an additional 3.0 hours. Step 4: The reaction temperature was lowered to 100° C. with a stirring speed of 250 rpm, and the Dean-Stark trap was removed under nitrogen. The temperature was set to 60° C. at the same time n-hexane (2.5 L) was added at a flow rate of 25 mL/min. After the addition of hexane was complete, the intermediate complex (IC) suspension was maintained at room temperature. ¹Anhydrous butanol is prepared by was purchased from Aldrich as an anhydrous 1-butanol assay of 99.8%, which was then treated with 3A molecular sieves for further removal of water.

The intermediate complex suspension was determined by ICP-OES to contain 0.296 M titanium and 0.618 M magnesium, which is a magnesium:titanium ratio of about 2.1. A combined 41 mL of ethanol (26 mL) and n-butanol (15 mL) were removed via the Dean-Stark trap. This amounts of ethanol and butanol were determined using ¹³C NMR. Assuming complete removal of ethanol, the resultant Ti—Mg complex may have a formula of 0.36 TiCl(OBu)₃.0.72 Mg(OEt)_(1.4)(OBu)_(0.6). After collection of the solids and drying, ICP-OES analysis indicated that it contained 6.39 wt % Ti and 6.56 wt % Mg, with theoretical amounts of 8.46 and 8.60, respectively. The balance of the solids is the alkoxides and halides. The FTIR spectra of the complex of Example 1 and Ti(OBu)₄ were obtained and the spectra show characteristic α-C—H stretch vibrations bond to Mg and Ti, suggesting the formation of the Ti—Mg complex.

Discussion of Example 1. In this analysis, the integral ratio between the alpha carbons of ethanol and butanol, assigned as C(b) and C(f), respectively, was used as the reference peaks. This result indicates the molar ratio between ethanol and butanol in the collected sample. By applying equation (1) is possible to estimate that approximately 26 mL of the collected sample was ethanol. Thus, assuming that most of the ethanol produced in step 2 reaction was collected, as shown in Scheme 1, it results in a molar conversion of 0.31 of the butanol-magnesium ethoxide exchange reaction.

$\begin{matrix} {\frac{\int\alpha_{c\; 2}}{\int\alpha_{c\; 4}} = \frac{\frac{\left( {V_{t} - {Vc}_{4}} \right) \cdot \rho_{c\; 2}}{\overset{\_}{M_{c\; 2}}}}{\frac{V_{c\; 2} \cdot \rho_{c\; 4}}{\overset{\_}{M_{c\; 4}}}}} & {{Equation}\mspace{14mu}(1)} \end{matrix}$ Where, ∫α_(c2 & c4) are the ¹³C NMR integral of the alpha carbon peaks, ρ_(c2 & C4) are the densities and M_(c4 & c2) are the molar masses of ethanol and butanol, respectively, V_(t) is the total volume collected in the Dean-Stark, Vc4 is the volume of butanol. Based on this information, it is possible to estimate the complex composition of Step 2 in Example 1, as shown in Scheme 2. Based upon the foregoing, the intermediate complex of Example 1 is: 0.36TiCl(O-n-Bu)₃.0.72Mg(O-Et)_(1.4)(O-n-Bu)_(0.6). The chemical formula is C_(8.06)H_(18.65)Cl_(0.36)Mg_(0.72)O_(2.52)Ti_(0.36) having a molecular weight of 203.46 g/mol.

Example 2

Step 1-2: Same as Example 1. Step 3: The reaction temperature was raised to 150° C. and the stirring speed to 500 rpm. This condition was maintained for 1.5 hours followed by the collection of byproducts in the Dean-Stark trap. Four extra additions of dehydrated n-butanol (4×25.0 mL, 4×0.27 mol) were then introduced at flow rate of 15 mL/min every 30 min for an additional 4.0 hours of reaction time. Step 4: Same as Example 1.

Under the conditions of Example 2, the intermediate complex suspension was determined by ICP-OES to contain 0.314 M titanium and 0.618 M magnesium, which is a magnesium:titanium ratio of about 2.0. A combined 58 mL of ethanol (39 mL) and n-butanol (19 mL) were removed via the Dean-Stark trap. The intermediate complex of Example 2 is: 0.36TiCl(O-n-Bu)₃.0.72Mg(O-Et)_(1.1)(O-n-Bu)_(0.9). The chemical formula is C_(8.50)H_(19.51)Cl_(0.36)Mg_(0.72)O_(2.52)Ti_(0.36) having a molecular weight of 209.35 g/mol. After collection of the solids and drying, ICP-OES analysis indicated that it contained 9.08 wt % Ti and 7.30 wt % Mg, with theoretical amounts of 8.20 and 8.33, respectively.

Example 3

Steps 1-4: Same as Example 1. The aim of this example is to reproduce the experiments on Example 1 and under these conditions reach concentration of 0.3 M titanium and 0.6 M magnesium, which gives a magnesium:titanium ratio of about 2.0. A combined 21 mL of ethanol (17 mL) and n-butanol (4 mL) were removed via the Dean-Stark trap. The intermediate complex of Example 3 is: 0.36TiCl(O-n-Bu)₃.0.72 Mg(O-Et)_(1.6)(O-n-Bu)_(0.4). The chemical formula is C_(7.78)H_(18.01)Cl_(0.36)Mg_(0.72)O_(2.52)Ti_(0.36) having a molecular weight of 199.27 g/mol. The FTIR spectra of the complex of Example 3 was obtained suspended in hexane and in the isolated form. The spectra show characteristic α-C—H stretch vibrations bond to Mg and Ti suggesting the formation of the Ti—Mg complex.

Summary of Examples 1-3. The intermediate complex preparation includes two main reaction steps, as shown in Scheme 1. Step 1 is an interchange reaction between titanium alkoxide and chloride to obtain a titanium alkoxy-halide complex. Step 2 is a suspension of the magnesium ethoxide into the titanium alkoxy-halide complex, which is promoted by the partial or complete exchange reaction between butanol and magnesium ethoxide to form magnesium butoxide. After the formation of a uniform, suspended Ti—Mg complex, it is then allowed to suspend in excess of hexane to reach concentrations of Ti lower than 0.4 mol/L and the suspension is maintained at 60° C. under stirring conditions for at least 1 hour before being allowed to cool to 25° C.

The concentration of Ti and Mg after the addition of hexane was estimated by ICP-OES. The Ti—Mg complex was suspended in approximately 2 L of hexane (1^(st) dilution). The results are shown in Table 2.

TABLE 2 Metal concentration in the intermediate complex suspension in hexane by ICP-OES. Sample [Ti] mol/L [Mg] mol/L [Mg]/[Ti] Example 1 0.296 0.618 2.1 Example 2 0.314 0.618 2.0 Example 3 n.d. n.d. n.d. n.d. = not determined.

It is important to notice that the molar concentration ratio between [Mg]/[Ti] in the first dilution obtained by ICP-OES is 2.0, which is the expected result as shown in the stoichiometric coefficients in Scheme 1.

The obtained suspensions were also analyzed by thermogravimetric analysis (TGA), optical microscopy, Focused Beam Reflectance Measurement (FBRM), Dynamic Light Scattering (DLS), and Electrophoretic Light Scattering (ELS).

TGA

Examples 1-3 were subjected to thermogravimetric analysis assuming the decomposition product is titanium and magnesium oxide. Example 1 has a theoretical weight loss of 71.61 wt % and a measured weight loss of 77.71 wt %. Example 2 has a theoretical weight loss of 72.49 wt % and a measured weight loss of 72.98 wt %. Example 3 has a theoretical weight loss of 71.01 wt % and a measured weight loss of 76.88 wt %.

Optical Microscopy

The Ti—Mg complex suspensions (Example 1 and 2) were transferred to a sample holder with a quartz window inside the glove box (under nitrogen) before the optical microscopy analysis. It has been observed that by increasing the content of the butoxide group in Example 2 appears to suppress the formation of aggregates in the micro-size range. As reported by D. C. Bradley (Chem. Rev. 89, 1317-1322 (1989)), alkoxides containing less sterically bulky groups (e.g., methyl and ethyl) proved to be oligomers (e.g., dimers, trimers, and tetramers) due to the bridging propensity of the alkoxide group, which may be bounded through its oxygen to two or three metals by means of conventional two-electron covalent bonds. Therefore, by increasing the bulkiness of the alkoxide group in Example 2 (higher content of butoxide over ethoxide), it seems to suppress the formation of large aggregates efficiently.

FBRM

The FBRM experiment is described by Yu, Z. Q. et al. Organic Process Research & Development 2008, 12, 646:

-   -   In Focused Beam Reflectance Measurement (FBRM), a focused laser         beam spinning at high speed propagates into slurry/suspension         through a sapphire window mounted on the tip of a cylindrical         probe. When the laser beam intersects the edge of a particle,         some of it is backscattered to the detector installed in the         same probe, and induces a rise signal in the circuit until it         reaches the opposite edge of the particle. A chord length is         thus registered. The product of risetime and tangential velocity         of the spinning laser beam is a chord length. The measurement         range of a chord length depends on the scanning speed of the         laser beam and is divided into a fixed number of linear channels         in the hardware. Each count of chord length is recorded in a         corresponding channel and a chord length distribution (CLD) is         thus generated. Chord length counts grouped by channels are the         primary data provided by FBRM. In addition, the control         interface provides a variety of weighted or unweighted         statistics of the primary data, e.g. total counts of chord         lengths in all channels, mean chord lengths, median standard         deviation of CLD, etc., which are different statistical         presentations of the primary data.

For the FBRM measurement conducted here, 1 L jacketed reactor equipped with an overhead stirrer and a portable FBRM® G600B from Mettler-Toledo was used. The FBRM® is a real-time quantitative measurement that tracks the rate and degree of change to particles, particle structures, and droplets in a medium. The G600B wetted probe dimensions (D×L) are 19 mm×400 mm built with a Hastelloy C22 and Sapphire window. The probe temperature operation range is −10° C. to 120° C. and a pressure limit of 10 bar. The intermediated complex suspension is transferred to the reactor and further diluted with hexane to reach a [Ti] of 0.125 mol/L. The mixture was then stirred at 250 rpm for 30 min at 30° C. prior to the measurement. The stirring was stopped, and the cord length of the particles of the material of Example 1 suspended domains in hexane was recorded as shown in FIG. 3. FIG. 4 illustrates that the suspension is stable over time at 30° C. and 40° C. without stirring.

The Ti—Mg complex suspensions were transferred to a sample holder with a quartz window inside the glove box (under nitrogen) for optical microscopy analysis.

DLS

All Dynamic Light Scattering (DLS) measurements were carried out in a Zetasizer NANO from Malvern Instruments using a quartz cell for the measurements. All the samples were prepared under an inert atmosphere, and the cell was capped during the measurement.

FIG. 5 is an illustration of the size distribution by intensity and volume of the Examples 1-3 suspension in hexane at 25° C. and [Ti] of 0.125 mol/L. Under this condition the samples showed a bimodal particle size by intensity distribution in the ranges shown in Table 3.

TABLE 3 Summary of DLS results of the material of Examples 1-3 as a suspension in hexane at [Ti] = 0.125 mol/L and 25° C. Examples Peak^(a), nm (Intensity, %) 1 2.33 (8.7); 294.3 (96.3) 2 2.70 (3.9); 396.0 (21.9) 3 2.33 (15.6); 122.0 (57.0)  ^(a)sizes are given in diameter ELS

All of the Electrophoretic Light Scattering (ELS) measurements were carried out in a Zetasizer NANO from Malvern Instruments using a solvent resistance cell in a quartz cuvette.

TABLE 4 Summary of ELS results of the material of Example 1 and 3 as a suspension in hexane at [Ti] = 0.125 mol/L. Examples Zeta Potential (mV) Mobility (μmcm/V · s) 1  −9.94 −0.03697 2 n.d. n.d. 3 −20.3 −0.07530 Measurement duration from 10-100 runs at 25° C. using hexane as a dispersant. The hexane refractive index is 1.390, viscosity 0.3 cP, and dielectric constant is 1.89.

Example 4

To a 1 L glass reactor equipped with a mechanical agitator, heated jacket, and reflux condenser under an inert atmosphere, 336 mL of the intermediate complex of Example 1 in hexane ([Ti]=0.296 mol/L) was added. The stirrer was set to 1500 rpm and the reactor temperature to 30° C. Under these conditions, 280.0 mL of ethyl aluminum sesquichloride (EASC) solution (50 wt % in hexane (0.47 mol)) was added at a flow rate of 5.00 mL/min. The obtained slurry mixture is then allowed to heat up to 60° C., and the reactive mixture is kept at this condition for 1 hour. Before starting the washing step, the reactor temperature was reduced to 40° C. The agitation was stopped, and the solid pre-catalyst was allowed to settle at the bottom of the reactor. The supernatant was removed by cannula to a quench vessel, and 500 mL of hexane was added. The slurry was stirred at 300 rpm for at least 15 min, and the step was repeated at least three more times before the final pre-catalyst slurry was transferred to a storage flask under an inert atmosphere. The results are shown in Table 5.

Example 5

Similar conditions of Example 4. The differences are: (a) Intermediate Complex of Example 1 in hexane [Ti]=0.205 mol/L to produce the pre-catalyst of this Example. The results are shown in Table 5.

Example 6

Similar conditions to Example 5 were used. However, the Intermediate Complex of Example 1 in hexane [Ti]=0.125 mol/L and a stirring speed of 1700-1800 rpm were used to produce the pre-catalyst. The results are shown in Table 5.

Example 7

Similar conditions to Example 6 were used. However, a stirring speed of 1800 rpm, a reaction temperature of 40° C., and an EASC flow rate of 1-2 mL/min were used. The results are shown in Table 5.

Example 8

Similar conditions to Example 7 were used. However, the reaction temperature was 30° C. The results are shown in Table 5.

Example 9

Similar conditions to Example 8 were used. However, the reaction temperature was 60° C., and a stirring speed of 500 rpm was used. The results are shown in Table 5.

Example 10

Similar conditions to Example 8 were used. However the Intermediate Complex of Example 1 in hexane [Ti]=0.076 mol/L, a reaction temperature of 30° C., a stirring speed of 1600 rpm, and a EASC volume of 140 mL were used. The results are shown in Table 5.

Example 11

Similar conditions to Example 8 were used. However a stirring speed of 1100 rpm was used. The results are shown in Table 5.

Example 12

Similar conditions to Example 10 were used. However the Intermediate Complex of Example 1 in hexane [Ti]=0.125 mol/L, a reaction temperature of 10° C., and an EASC volume of 280 mL were used. The results are shown in Table 5.

Example 13

Similar conditions to Example 12 were used. However the Intermediate Complex of Example 1 in hexane [Ti]=0.076 mol/L, a reaction temperature of −10° C., and an EASC volume of 140 mL were used. The results are shown in Table 5. FIG. 13 illustrates the particle size distribution measured in a Mastersizer 2000 laser diffraction particle size analyzer from Malvern Panalytical, for Examples 7, 11, and 12.

Note that in each of Examples 4-14, a setup as illustrated in FIG. 10A was used.

TABLE 5 Summary of pre-catalyst synthesis conditions using feeding method A. Ti-Mg complex Stirring EASC^(d) suspension Speed T Volume Flow rate —Cl/-OR Pre-catalyst (mol_(Ti)/L)^(a) (rpm) (° C.)^(c) (L) (ml/min) mol/mol 4 0.293 1500 30 0.28 5 2.9 5 0.205 1500 30 0.28 5 3.7 6 0.125 1700-1800^(b) 30 0.23 5 5.0 7 0.125 1800 40 0.23 1-2^(e) 5.0 8 0.125 1800 30 0.23 1-2^(e) 5.0 9 0.125  500 60 0.23 1-2^(e) 5.0 10 0.076 1600 30 0.14 1-2^(e) 5.0 11 0.125 1100 30 0.23 1-2^(e) 5.0 12 0.125 1600 10 0.23 1-2^(e) 5.0 13 0.076 1600 −10 0.14 1-2^(e) 5.0 ^(a)Ti-Mg complex suspension volume used in the preparation of pre-catalysts 4-6 was 0.335 L, and pre-catalysts 7-14 was 0.37 L; ^(b)stirring speed was increased after 35 min of reaction relative to the start of EASC transfer; ^(c)temperature during the addition of EASC; ^(d)50 wt % solution in hexane; ^(e)flow rate increased after 80 min of reaction relative to the start of EASC transfer.

Example 14

275 mL of hexane was transferred to 1 L glass reactor equipped with a mechanical agitator, heated jacket, and reflux condenser under an inert atmosphere. The stirrer was set to 1600 rpm and the reactor temperature to 30° C. Under these conditions was fed to the reactor simultaneously 95 mL of the Intermediate Complex of Example 1 in hexane ([Ti]=0.296 mol/L) at 1.35 mL/min and 140.0 mL of ethyl aluminum sesquichloride (EASC) solution (50 wt % in hexane (0.235 mol)) at flow rate of 2.00 mL/min. The obtained slurry mixture is then allowed to heat up to 60° C., and the reactive mixture was kept at this condition for 1 hour. Before starting the washing step, the reactor temperature was reduced to 40° C. The agitation was stopped, and the solid pre-catalyst was allowed to settle at the bottom of the reactor. The supernatant was removed by cannula to a quench vessel, and 500 mL of hexane was added. The slurry was stirred at 300 rpm for at least 15 min, and the step was repeated at least three more times before the final pre-catalyst slurry was transferred to a storage flask under an inert atmosphere. The results are shown in Table 6.

Example 15

Similar conditions to Example 14 were used. However the Intermediate Complex of Example 2 in hexane [Ti]=0.314 mol/L and stirring condition of 1100 rpm were used. The results are shown in Table 6.

Example 16

Similar conditions to Example 15 were used. However the stirring condition of 500 rpm was used. The results are shown in Table 6.

Example 17

Similar conditions to Example 15 were used. However the stirring condition of 1500 rpm was used. The results are shown in Table 6.

Example 18

Similar conditions to Example 15 were used. However the stirring condition of 1600 rpm was used. The results are shown in Table 6.

Example 19

Similar conditions to Example 18 were used. However the reaction temperature of −10° C. was used. The results are shown in Table 6.

Example 20

Similar conditions to Example 18 were used. However the reaction temperature of 60° C. was used. The results are shown in Table 6.

Therefore, two different methods for pre-catalyst preparation were explored in the examples above. Examples 4-14 use the addition of the halogenated compound (EASC) into the Ti—Mg suspension, as shown in FIG. 10A. Differently, examples 14-20 use the co-addition of the halogenated compound (EASC) and Ti—Mg complex suspension into a specific volume of hexane to enable mixing conditions, as shown in FIG. 10B. Note that by the pre-catalyst preparation method B (co-addition), the concentration of Ti derived from the Ti—Mg complex is rapidly consumed over the reaction time, as exemplified in FIG. 7. As a result of this approach, a more pronounced dilution effect to the pre-catalyst particle size formation can be observed, as shown in FIG. 8.

TABLE 6 Summary of pre-catalyst synthesis conditions using feeding method B. Reactor Conditions IC EASC Stirring Flow Flow Hexane Speed T [Ti] Volume rate Volume rate Pre-catalyst (L) (rpm) (° C.) (mol/L) (L) (ml/min) (L) (ml/min) 14 0.275 1600 30 0.296 95 1.35 0.14 2.0 15 0.275 1100 30 0.314 95 1.35 0.14 2.0 16 0.275 500 30 0.314 95 1.35 0.14 2.0 17 0.275 1500 30 0.314 95 1.35 0.14 2.0 18 0.275 1600 30 0.314 95 1.35 0.14 2.0 19 0.275 1600 −10 0.314 95 1.35 0.14 2.0 20 0.275 1600 60 0.314 95 1.35 0.14 2.0

Table 7 illustrates is a summary of catalyst particle size and composition for Examples 4-20.

Chemical composition^(b) Pre-catalysts D₅₀ ^(a) (μm) Mg (wt %) Ti (wt %) Al (wt %) 4 8.9 7.5 7.3 2.6 5 10.6 6.7 6.2 2.2 6 7.8 8.7 6.3 3.0 7 8.9 13.0 13.6 4.6 8 8.0 9.2 11.3 4.0 9 21.9 10.0 8.4 4.6 10 7.5 10.5 11.1 4.4 11 14.4 9.3 10.2 3.5 12 6.7 8.3 9.3 3.6 13 4.5 11.1 10.2 5.0 14 4.0 12.2 13.8 3.9 15 5.9 10.5 16.9 3.9 16 7.9 9.3 11.6 2.8 17 4.8 7.4 11.6 2.9 18 3.7 10.0 11.7 3.5 19 5.3 9.3 10.1 3.7 20 3.2 10.2 12.4 3.9 ^(a)Off-line particle size measurement carried out by small-angle static scattering (SASLS) in a Mastersizer ® 2000 (Malvern). ^(b)Determined by ICP-OES from a dried pre-catalyst powder.

This is also a significant benefit to producing small particle size pre-catalysts by using the pre-catalyst preparation method B (FIG. 10B) over the pre-catalyst preparation method A (FIG. 10A). As shown in FIG. 11, the smaller pre-catalyst particle size range was obtained under similar shear rate conditions independently of the intermediate complex used in the Example 14-20 (pre-catalyst preparation method B). In other words, much less energy input was required to produce smaller pre-catalyst particle size in the pre-catalyst preparation method B (FIG. 10B).

Example 21

Ethylene polymerization was performed in a one-gallon reactor. The reactor was purged at 100° C. under nitrogen for one hour. At room temperature, the reactor is charged with 2.3 L of hexane and 230 mg of DEAC (diethyl aluminum). Then, 30 mg of pre-catalyst in hexane slurry is added into the reactor. The reactor temperature was increased to 80° C. and then charged with ethylene to reach 120 psi. The pressure is kept constant with ethylene pressure until 360 g of ethylene is consumed. At the end of the hold, the reactor was vented, and the polymer was recovered. The results are listed in Tables 8 and 9.

TABLE 8 Summary of the catalyst performance. Polymerization time Pre-catalyst^(a) Yield CE^(c) Catalyst (min) (mg) (g) (kg_(PE) · g_(Cat) ⁻¹ · h⁻¹) 4 64 30^(a) 346 11 5 59 30^(a) 350 12 6 71 30^(a) 349 10 7 94 30^(a) 317 7 8 132 30^(a) 313 5 9 68 30^(a) 330 10 10 87 25^(b) 346 10 11 88 26^(b) 307 8 12 86 31^(b) 329 7 13 60 20^(b) 181 9 14 120 16^(b) 285 9 15 136 30^(a) 248 4 16 142 30^(a) 124 2 17 60 30^(a) 377 12 18 60 30^(a) 402 13 19 60 30^(a) 124 4 20 60 30^(a) 257 10 ^(a)Experimental pre-catalyst amount is 30 mg; ^(b)Determined by ICP-OES; ^(c)CE is an abbreviation for Catalyst Efficiency in units of (kg of polymer)/g pre-catalyst/hour).

TABLE 9 Polymer properties Polymers from above using the BD IV MW D₅₀ materials of Catalyst (g/cm³) (dl/g) (10⁻⁶ g/mol) (μm) 4 0.391 26.1 6.92 179.0 5 0.339  6.4 0.86 227.9 6 0.351 15.6 3.22 208.0 7 0.423 29.9 8.50 226.0 8 0.402 26.6 7.14 196.2 9 0.320 22.2 5.46 582.6 10 0.376 24.8 6.44 177.0 11 0.379 24.6 6.34 293.3 12 0.405 24.3 6.22 149.0 13 0.311 18.8 4.25 119.0 14 0.312 23.1 5.76 119.0 15 0.263 20.5 4.83 122.5 16 0.297 29.0 8.11 n.d. 17 0.227 n.d. n.d. 111.0 18 0.307 21.1 5.03 107.0 19 0.230 23.1 5.79  79.5 20 0.193 n.d. n.d. n.d. ^(a)Intrinsic viscosity measurements as described in ASTM D-4020. ^(b)Viscosity molecular weight was estimated from Margolies equation, which is based on Mark-Houwink parameters for polymer-solvent systems.

Example 22

Polymerization reactions were carried under similar conditions to Example 21. However, polymerization time was fixed to 30 min, and pre-catalyst systems underwent different activation conditions, as shown in Table 10. In this case, the polymerization reactor was charged with different levels of DEAC, TiBA, and the mixture of both co-catalysts under different molar ratio. The results are also summarized in FIG. 12A-B.

TABLE 10 Summary of polymerization conditions, catalyst performance results, and polymer properties. Co-catalyst Co-catalyst CE^(c) BD, MW, D₅₀, Pre-catalyst^(a) Type (mmol) (kg_(PE) · g_(Cat) ⁻¹ · h⁻¹) (g/cm³) (10⁻⁶ g/mol) (μm) 12 DEAC 2.8 12.40 0.317 5.29 88 3.8 13.33 0.296 4.67 88 4.8 13.33 0.306 4.65 92 12 TiBA 1.5 13.53 0.271 4.04 104 2.1 13.07 0.282 4.21 98 2.7 12.80 0.276 3.71 98 13 DEAC 2.8 13.07 0.256 5.45 103 3.8 8.60 0.235 5.80 111 4.8 13.33 0.266 5.13 106 13 TiBA 1.5 12.87 0.272 3.67 106 2.1 13.47 0.262 3.60 105 2.7 13.20 0.246 3.45 107 12 DEAC/TiBA 2.2/0.6 12.97 0.280 4.85 98 1.4/1.4 13.06 0.285 5.95 94 0.6/2.2 14.11 0.270 4.63 102 13 DEAC/TiBA 2.2/0.6 13.07 0.261 3.45 89 1.4/1.4 13.60 0.268 3.98 113 0.6/2.2 12.93 0.276 4.97 97 ^(a)Target pre-catalyst feed was 30 mg.

Example 23

A general polymerization procedure was carried out in a reactor cell with a geometric volume of approximately 23 mL and a working volume of approximately 5.5 mL for the liquid phase equipped with a magnetically coupled mechanical stirrer. The cell was initially purged under intermittent nitrogen flow at 90° C. to 140° C. for 8 hours. After then cooling to room temperature, the cell was fitted with disposable 10 mL glass and stir paddles, and the stir tops were then set back in the reactor system. The amount of dried heptane and 1-butene as co-monomer was then fed through a syringe pump to the reactor system with the presence of small amounts of alkyl aluminum as a scavenger. The system was then allowed to reach the set temperature and operating pressure with ethylene, which general working pressure was 120 psi. Under this condition, using a slurry needle system, the amount of pre-catalyst dispersed in heptane slurry (approx. 0.1 mg) was collected. A solution of alkyl aluminum, usually the same used as a scavenger, in heptane was charged to the needle system before being injected into the cell. The polymerization reaction starts under constant pressure by feeding ethylene and stirring (800 rpm), typically for 30 min. The reaction was quenched by over-pressurizing the system with dry air, and the reactor was cooled to room temperature and vented. The glass cell was removed from the reactor, the solvent evaporated in a centrifugal evaporator, and the obtained polymer dried under vacuum overnight.

The polymerization results are summarized in Table 11 for the tested catalyst system.

TABLE 11 Summary of polymerization conditions. 1-Butene CE^(c) Pre-catalyst^(a) Co-catalyst Type (mmol) (kg_(PE) · g_(Cat) ⁻¹ · h⁻¹) 12 DEAC 0.5 10.4 1.1 11.3 1.6 11.3 12 TiBA 0.6 28.1 1.1 9.7 1.6 6.2 13 DEAC 0.5 13.0 1.1 10.5 1.6 5.8 13 TiBA 0.5 25.2 1.1 9.6 1.6 3.0 14 DEAC 0.5 8.7 1.1 5.4 1.6 2.8 14 TiBA 0.5 19.4 1.1 14.0 1.6 18.8

Example 24

The effect of temperature and mixing on particle size was studied. As shown in FIG. 14, three different operations are described. It has been found that differences in the mechanisms of pre-catalyst formation, feeding methods B and C have a very distinguished temperature response to pre-catalyst particle size compared to method A. It has been found that the pre-catalyst particle size is decreased by increasing the temperature of the medium when reactants feeding methods B and C are used, as shown in FIG. 15. The preparation conditions of the pre-catalysts system under different reaction temperature is summarized in Table 12.

TABLE 12 Summary of the pre-catalyst preparation examples under different methods. IC Suspension EASC [Ti], Volume, Flow rate, T, Volume, Flow rate, Method^(a) Examples mol/L L mL/min ° C. L mL/min Method B^(b) 18 0.314 0.095 1.35 30 0.14 2.0 25 0.314 0.095 1.35 −10 0.14 2.0 26 0.314 0.095 1.35 60 0.14 2.0 Method C 27 0.314 0.095 1.0 30 0.415 n.a. 28 n.d. 0.095 1.0 30 0.415 n.a. 29 n.d. 0.095 1.0 60 0.415 n.a. 30 n.d. 0.095 1.0 −10 0.415 n.a. 31 n.d 0.095 1.0 −10 0.415 n.a. ^(a)All examples were carried out at stirring speed of 1600 rpm; ^(b)275 mL of hexane was used as an inert medium for the co-addition; ^(c)flow rate increased after 80 min of reaction relative to the start of EASC addition.

TABLE 13 Summary of pre-catalyst particle size and metal composition Feeding Mode Chemical composition method Pre-Catalyst (μm)^(a,b) Mg (wt %) Ti (wt %) Al (wt %) Method B 18 3.8 10.0 11.7 3.5 25 5.5 9.3 10.1 3.7 26 3.3 10.2 12.4 3.9 Method C 27 5.5 9.3 11.5 3.7 28 5.5 n.d n.d. n.d. ^(a)Off-line particle size measurement carried out by small-angle static scattering (SASLS) in a Mastersizer ® 2000 (Malvern). ^(b)Mode refers to the highest peak seen in the distribution and used in these cases due to the multimodality of the distributions in Method C. ^(c)Determined by ICP-OES from a dried pre-catalyst powder

Method A. To a 1 L glass reactor equipped with a mechanical agitator, heated jacket, and reflux condenser under an inert atmosphere, 375 mL of the intermediate complex suspension in hexane ([Ti]˜0.3 mol/L) is added. At mixing speed of 1600 rpm the desired temperature is set from −10° C. to 60° C. Under these conditions, 230.0 mL of EASC 50 wt % in hexane is added at 1.0-2.0 mL/min. The obtained pre-catalyst slurry is then allowed to heat up to 60° C., and the reactive mixture is kept at this condition for 1 hour. Before starting the washing step, the reactor temperature is reduced to 40° C. The agitation was stopped, and the solid pre-catalyst is allowed to settle at the bottom of the reactor. The supernatant is removed by cannula to a quench vessel, and 500 mL of hexane is added. The slurry is stirred at 300 rpm for at least 15 min, and the step is repeated at least three more times before the final pre-catalyst slurry is transferred to a storage flask under an inert atmosphere.

Method B. Hexane (275 mL) was transferred to 1 L glass reactor equipped with a mechanical agitator, heated jacket, and reflux condenser under an inert atmosphere. At stirring speed of 1600 rpm the desired temperature is set from −10° C. to 60° C. Under these conditions, 95 mL of the intermediate complex suspension in hexane ([Ti]˜0.3 mol/L) at 1.35 mL/min and 140.0 mL of EASC 50 wt % in hexane at a flow rate of 2.00 mL/min are fed to the reactor, simultaneously. The obtained slurry mixture is then allowed to heat up to 60° C., and the reactive mixture is kept at this condition for 1 hour. Before starting the washing step, the reactor temperature was reduced to 40° C. The agitation was stopped, and the solid pre-catalyst is allowed to settle at the bottom of the reactor. The supernatant is removed by cannula to a quench vessel, and 500 mL of hexane is added. The slurry is stirred at 300 rpm for at least 15 min, and the step is repeated at least three more times before the final pre-catalyst slurry is transferred to a storage flask under an inert atmosphere.

Method C. To a 1 L glass reactor equipped with a mechanical agitator, heated jacket, and reflux condenser under an inert atmosphere, 415 mL of the EASC 19 wt % solution in hexane is added at room temperature. The stirring speed of 1600 rpm and reactor temperature from −10° C. to 60° C. is then set. Under these conditions, 90.0 mL of intermediate complex suspension in hexane ([Ti]˜0.3 mol/L) is added at flow rate of 1.00 mL/min. The obtained pre-catalyst slurry is then allowed to heat up to 60° C., and the reactive mixture is kept at this condition for 1 hour. Before starting the washing step, the reactor temperature is reduced to 40° C. The agitation was stopped, and the solid pre-catalyst is allowed to settle at the bottom of the reactor. The supernatant is removed by cannula to a quench vessel, and 500 mL of hexane is added. The slurry is stirred at 300 rpm for at least 15 min, and the step is repeated at least three more times before the final pre-catalyst slurry is transferred to a storage flask under an inert atmosphere.

Particle formation over the course of the pre-catalyst synthesis was monitored using a ParticleView V19 from Metller-Toledo. This probe enabled an image-based monitoring of the particle formation and tracks change in turbidity image analysis as a function of image brightness and the intensity of the light source. The turbidity image analysis profiles of the pre-catalyst synthesis as a function of the reaction temperature using reactants feeding Method C is shown in FIG. 16. In these experiments, the turbidity unity (TU) from the image analysis is a function of particle size and solid concentration, which is changed by the temperature of the reaction medium. Other important parameters, such as particle shape, particle brightness, refractive index, and all reaction process parameters (i.e., stirring speed, feed rate, the concentration of the reactants and source of reactants) are kept the same among the selected experiments.

In a different embodiment, the Turbidity Unity (TU) relative to the image analysis obtained from PVM V19 probe was modeled using equation (2), where k_(T)(T) is the TU time constant and is a function of reactor operating temperature, and TU_(max)(T) is the maximum TU for the system, and it is also a function of reactor temperature, as shown in FIG. 17. Equation (2) reflects the onset of change in turbidity in the reactive medium to the completion of the IC feeding in the pre-catalyst preparation Method C.

$\begin{matrix} {\frac{dTU}{dt} = {{k_{T}(T)}\left( {{T{U_{\max}(T)}} - {TU}} \right)}} & {{Equation}\mspace{14mu}(2)} \end{matrix}$

The values for k_(T) and TU_(max) for each experimental run were determined by formulating and solving a nonlinear programming problem (NLP) where the objective is to minimize the mean squared error between measured and calculated TU vales. Equation (2) was integrated in time by means of orthogonal collocation on finite elements using three Lagrange-Radau collocation points, and the temperature was assumed to be constant for each experimental run. The NLP is represented in equation (3), and it was implemented in Pyomo and solved using IPOPT 3.12.13. The values for k_(T) and TU_(max) are presented in Table 1 at each.

$\begin{matrix} {{\min\limits_{k_{T},{TU}_{\max}}{\sum\limits_{k}^{NFE}{{{TU}_{(k)} - {TU}_{(k)}^{*}}}^{2}}}{{s.t.\mspace{11mu}{TU}_{({k + 1})}} = {f\left( {{TU}_{(k)},T} \right)}}} & {{Equation}\mspace{14mu}(3)} \end{matrix}$

TABLE 14 Model Parameters at different temperatures Pre-catalysts Reaction Temperature k_(T), 1/hour TU_(max) ^(a) 30 −10° C. 2.12154012 0.5942200306 28 30° C. 2.49112764 0.7696509401 29 60° C. 3.14570016 0.8655988585 ^(a)turbidity units relative to image analysis obtained from PVM V19 probe.

The functions k_(T)(T) and TU_(max)(T) are defined by the second order polynomial defined by equation (4) and equation (5): k _(T)(T)=0.0001797*T ²+0.005646*T+2.16  Equation (4) TU_(max)(T)=−1.696e−05*T ²+0.004725*T+0.6432  Equation (5)

Example 32

Same initial workup procedure as Example 23, but in these experiments, the amount of dried heptane was initially fed through a syringe pump to the reactor system with the presence of 1.0 μmol of DEAC as a scavenger. The system was then allowed to reach the set temperature (from 65-100° C.) and operating pressure with hydrogen and ethylene, which general working pressure ranged from 110-135 psi. Under this condition, using a slurry needle system, the amount of pre-catalyst dispersed in heptane slurry (approx. 0.03 mg) was collected. A solution containing 3.6 μmol of DEAC in heptane was charged to the needle system before being injected into the cell. The polymerization reaction starts under constant pressure by feeding ethylene and stirring (800 rpm), typically for no longer than 60 min. The reaction was quenched by over-pressurizing the system with dry air, and the reactor was cooled to room temperature and vented. The glass cell was removed from the reactor, the solvent evaporated in a centrifugal evaporator, and the obtained polymer dried under vacuum overnight.

TABLE 15 Summary of polymerization conditions Run, Temperature, P_(C) ₂ _(H) ₄, P_(H) ₂ , CE, kg_(PE) · Pre-catalyst^(a) # ° C. psi psi g_(Cat) ⁻¹ · h⁻¹ 18 P1 65 105 5 9.4/9.5 P2 100 10 8.6/5.5 P3 90 20 6.0/6.3 18 P4 75 105 10 13.6/13.7 P5 95 20 11.2/6.7  P6 75 40 6.1/5.7 18 P7 85 115 10 15.5/18.4 P8 105 20 13.7/14.5 P9 85 40 7.9/7.9 18 P10 100 125 10 14.1/14.6 P11 115 20 11.0/7.5  P12 95 40 8.2/8.0 13 P13 65 105 5 6.8/8.2 P14 100 10 6.3/6.0 P15 90 20 5.1/5.2 13 P16 75 105 10 4.7/6.9 P17 95 20 7.2/7.0 P18 75 40 3.6/3.7 13 P19 85 115 10  8.0/17.3 P20 105 20  5.3/12.8 P21 85 40 7.5/7.7 13 P22 100 125 10  5.4/11.1 P23 115 20 11.4/7.7  P24 95 40 8.0/8.0 30 P25 65 105 5 4.3/4.5 P26 100 10 3.5/3.6 P27 90 20 3.2/3.5 30 P28 75 105 10 4.0/4.3 P29 95 20 4.6/1.9 P30 75 40 2.8/2.8 30 P31 85 115 10 8.5/6.4 P32 105 20 6.7/5.2 P33 85 40 3.8/4.1 30 P34 100 125 10 12.9/8.2  P35 115 20 9.1/4.0 P36 95 40 3.8/3.2 ^(a)Feed in hexane slurry.

The polymerization results are summarized in Table 16 for the tested catalyst system. The obtained polymers were then characterized by high temperature size exclusion chromatography (HSEC) and crystallization elution fractionation (CEF).

TABLE 16 Summary of the obtained polymer properties. Run, HSEC CEF Catalyst # M_(n), kDa M_(w), kDa M_(w)/M_(n) X_(Tel<30° C.) ^(A), wt % X_(Tel>85° C.) ^(B), wt % 18 P1 197/229 1082/1029 5.5/4.5 0.1 97.4 P2 n.d. n.d. n.d. n.d. n.d. P3 114/104 608/639 5.3/6.2 0.2 98.6 18 P4 131/151 757/760 5.8/5.0 n.d. n.d. P5 79/88 488/541 6.2/6.1 0.1 99.7 P6 40/41 279/313 6.9/7.6 0.6 98.8 18 P7 98/102 669/608 6.9/6.0 <0.1 99.3 P8 66/91 411/476 6.2/5.2 0.4 99.2 P9 29/32 219/225 7.6/7.0 0.6 98.5 18 P10 88/83 521/408 5.9/4.9 0.8 98.8 P11 63/33 255/185 4.1/5.6 0.7 98.9 P12 34/39 164/151 4.8/3.9 0.9 98.4 13 P13 194/208 1197/1180 6.2/5.7 0.3 97.5 P14 179/176 898/960 5.0/5.5 0.4 98.5 P15 125/98 699/682 5.6/6.9 0.3 98.0 13 P16 122/92 724/781 5.9/8.5 n.d. n.d. P17 87/89 521/525 6.0/5.9 0.2 99.2 P18 44/47 283/276 6.4/5.9 0.4 99.3 13 P19 117/109 678/533 5.8/4.9 0.8 97.8 P20 95/55 474/395 5.1/7.1 0.7 98.6 P21 34/36 234/238 6.9/6.5 0.9 97.9 13 P22 90/93 445/421 5.0/4.5 0.9 98.8 P23 59/75 268/321 4.6/4.3 0.6 99.1 P24 34/41 128/181 3.8/4.4 0.9 98.1 30 P25 133/125 773/680 5.8/5.4 0.2 98.7 P26 105/83 595/700 5.7/8.4 0.2 98.9 P27 67/72 372/391 5.5/5.4 0.3 99.0 30 P28 71/70 509/511 7.1/7.3 0.2 99.6 P29 52/43 276/286 5.3/6.6 0.3 99.4 P30 37/31 164/169 4.5/5.4 0.6 98.7 30 P31 69/66 410/349 5.9/5.2 0.4 99.4 P32 56/63 280/287 5.0/4.6 0.5 99.0 P33 28/33 193/150 6.9/4.6 1.0 98.0 30 P34 71/64 347/306 4.9/4.8 0.6 98.9 P35 41/44 209/237 5.2/5.4 0.6 98.6 P36 19/29 112/132 5.8/4.6 2.1 96.2

Para. 1. A complex of Formula I: XTiCl_(p)(OR¹)_(4-p).YMg(OR²)_(q)(OR³)_(t)  (I) wherein: a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; and R² is not the same as R³.

Para. 2. The complex of Para. 1, wherein R¹ is a C₃-C₆ alkyl, R² is C₂-C₄ alkyl, and R³ is a C₃-C₆ alkyl.

Para. 3. The complex of Para. 1 or 2, wherein R¹ is n-butyl, R² is ethyl, and R³ is n-butyl.

Para. 4. The complex of any one of Paras. 1-3, wherein p is 1.

Para. The complex of any one of Paras. 1-4, wherein q is from about 0.5 to 1.5, and t is from about 0.5 to 1.5.

Para. 6. The complex of any one of Paras. 1-5, wherein X is 0.2 to 0.5 and Y is 0.6 to 0.8.

Para. 7. The complex of any one of Paras. 1-6, wherein the molar ratio of X:Y is from 1 to 3.

Para. 8. The complex of any one of Paras. 1-7, wherein the molar ratio of X:Y is about 2.

Para. 9. The complex of any one of Paras. 1-8 that exhibits a ¹³C NMR spectra having an alkoxide resonance from 50 ppm to 80 ppm versus residual solvent signal of deuterated toluene-d₈.

Para. 10. The complex of any one of Paras. 1-9 that exhibits a ¹³C NMR spectra having an aryloxide resonance from 40 ppm to 120 ppm versus residual solvent signal of deuterated toluene-d₈.

Para. 11. The complex of any one of Paras. 1-10, wherein weight residue obtained by thermal gravimetric analysis (TGA) is from 20 wt % to 35 wt %.

Para. 12. The complex of any one of Paras. 1-11, which exhibits a Fourier Transform Infrared C—H stretching vibration at a wavenumber from 2500 cm⁻¹ to 4000 cm⁻¹.

Para. 13. A colloidal suspension comprising an organic solvent and a complex of Formula I: XTiCl_(p)(OR¹)_(4-p).YMg(OR²)_(q)(OR³)_(t)  (I) wherein: a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; and R² is not the same as R³.

Para. 14. The colloidal suspension of Para. 13, wherein the organic solvent comprises an alkane, aromatic, or a mixture of any two or more thereof.

Para. 15. The colloidal suspension of Para. 13 or 14, wherein the organic solvent comprises n-hexane, n-pentane, cyclohexane, toluene, benzene, benzine, o-cresol, p-cresol, m-cresol, 1,2-dimethylbenzene, 1,3-dimethylbenzene, 1,4-dimethylbenzene, ethylbenzene, cumine, trichloroethylene, trichlorobenzene, o-dichlorobenzene, or a mixture of any two or more thereof.

Para. 16. The colloidal suspension of any one of Paras. 13-15, wherein the complex exhibits a multimodal domain size of a dispersed phase.

Para. 17. The colloidal suspension of Para. 16, wherein the concentration of the Ti and Mg is from 1×10⁻⁵M to 2.0 M, as determined by inductively coupled plasma-optical emission spectrometry (ICP-OES).

Para. 18. The colloidal suspension of Para. 16 or 17, wherein the multimodal domain size exhibits a first peak with a domain size mean from 1 nm to 10 nm in diameter, and a second peak with a domain size mean from 250 nm to 350 nm in diameter at 20° C.

Para. 19. The colloidal suspension of Para. 16, 17, or 18, wherein the multimodal domain size exhibits a first peak with a domain size mean from 250 nm to 400 nm in diameter, and a second peak with a domain size mean from 4000 nm to 6000 nm in diameter at 50° C.

Para. 20. The colloidal suspension of Para. 16, 17, 18, or 19, wherein the multimodal domain size exhibits a first peak when measured by Focus Beam Reflectance Measurement (FBRM) with a cord length mean from 1 μm to 10 μm, when measured from −30° C. to 60° C.

Para. 21. A solid pre-catalyst system comprising solid particles of a composite of a reaction product of a halogenated compound and a colloidal suspension of a complex of Formula I: XTiCl_(p)(OR¹)_(4-p).YMg(OR²)_(q)(OR³)_(t)  (I) wherein: a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; and R² is not the same as R³.

Para. 22. The solid pre-catalyst system of Para. 21, wherein the halogenated compound comprises diethyl aluminum chloride (DEAC), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), titanium tetrachloride (TiCl₄), silicon tetrachloride (SiCl₄) or a mixture of any two or more thereof.

Para. 23. The solid pre-catalyst system of Para. 21 or 22, wherein the Ti is present from 0.5 wt % to 30 wt %.

Para. 24. The solid pre-catalyst system of any one of Paras. 21-23, wherein the Mg is present from 1 wt % to 20 wt %.

Para. 25. The solid pre-catalyst system of any one of Paras. 21-24, wherein the Al is present from 1 wt % to 20 wt %.

Para. 26. The solid pre-catalyst system of any one of Paras. 21-25, wherein the solid particles exhibit a D₅₀ from 1 μm to 30 μm.

Para. 27. The solid pre-catalyst system of any one of Paras. 21-26 further contacting with a reducing agent.

Para. 28. A method of polymerizing or co-polymerizing an olefin monomer, the method comprising: contacting a solid pre-catalyst system comprising solid particles of a composite of a reaction product of a halogenated compound and a colloidal suspension of a complex of Formula I with a reducing agent and the olefin monomer: XTiCl_(p)(OR¹)_(4-p).YMg(OR²)_(q)(OR³)_(t)  (I) wherein: a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; and R² is not the same as R³.

Para. 29. The method of Para. 28, wherein the reducing agent comprises diethyl aluminum chloride (DEAC), triethyl aluminum (TEA), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), triisobutyl aluminum (TiBA), trimethyl aluminum (TMA), methylaluminoxane (MAO), or a mixture of any two or more thereof.

Para. 30. The method of Para. 28 or 29, wherein the olefin monomer comprises ethylene, propylene, 1-butene, 4-methyl-1-pentene, 1-hexene, 1-octene, or a mixture of any two or more thereof.

Para. 31. The method of any one of Paras. 28-30, wherein the solid catalyst system exhibits a catalyst efficiency (CE) of greater than 2 kg_(PE)·g_(Cat) ⁻¹·h⁻¹.

Para. 32. The method of any one of Paras. 28-31, wherein the olefin is ethylene, and the method further comprises collecting polyethylene exhibiting an intrinsic viscosity of greater than 1.0 dl/g.

Para. 33. A method of forming a solid pre-catalyst system composition, the method comprising: contacting simultaneously a halogenated compound and a colloidal suspension of a complex of Formula I into an inert liquid medium to form the solid pre-catalyst system: XTiCl_(p)(OR¹)_(4-p).YMg(OR²)_(q)(OR³)_(t)  (I) wherein: a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; and R² is not the same as R³.

Para. 34. The method of Para. 33, wherein the organic solvent comprises an alkane, aromatic, or a mixture of any two or more thereof.

Para. 35. The method of Para. 33 or 34, wherein the organic solvent comprises n-hexane, n-pentane, cyclohexane, toluene, benzene, benzine, o-cresol, p-cresol, m-cresol, 1,2-dimethylbenzene, 1,3-dimethylbenzene, 1,4-dimethylbenzene, ethylbenzene, cumine, trichloroethylene, trichlorobenzene, o-dichlorobenzene, or a mixture of any two or more thereof.

Para. 36. The method of any one of Paras. 33-35, wherein the complex of Formula I exhibits a multimodal domain size of a dispersed phase.

Para. 37. The method of any one of Paras. 33-36, wherein the concentration of the Ti and Mg is from 1×10⁻⁵M to 2.0 M, as determined by inductively coupled plasma-atomic emission spectrometry (ICP-OES).

Para. 38. The method of any one of Paras. 36-37, wherein the multimodal domain size exhibits a first peak with a domain size mean from 250 nm to 400 nm in diameter, and a second peak with a domain size mean from 4000 nm to 6000 nm in diameter at 50° C.

Para. 39. The method of any one of Paras. 33-38, wherein the halogenated compound comprises diethyl aluminum chloride (DEAC), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), titanium tetrachloride (TiCl₄), silicon tetrachloride (SiCl₄) or a mixture of any two or more thereof.

Para. 40. The method of any one of Paras. 33-39, wherein the halogenated compound is diluted in an organic solvent at a concentration of greater than 5 wt %.

Para. 41. The method of any one of Paras. 33-40, wherein the inert liquid medium comprises an alkane, aromatic, or a mixture of any two or more thereof.

Para. 42. The method of any one of Paras. 33-41, wherein the inert liquid medium comprises n-hexane, n-pentane, cyclohexane, toluene, benzene, benzine, o-cresol, p-cresol, m-cresol, 1,2-dimethylbenzene, 1,3-dimethylbenzene, 1,4-dimethylbenzene, ethylbenzene, cumine, trichloroethylene, trichlorobenzene, o-dichlorobenzene, mineral oil, or a mixture of any two or more thereof.

Para. 43. The method of any one of Paras. 33-42, wherein a temperature of the inert liquid medium is from −40° C. to +60° C.

Para. 44. The method of any one of Paras. 33-43, wherein the contacting comprises stirring at 50 rpm to 1800 rpm.

Para. 45. The method of any one of Paras. 33-44, wherein the contacting comprises simultaneous addition of the halogenated compound(s) and the colloidal suspension of a complex of Formula I is at a constant chloride to —OR^(x) molar ratio, where R^(x) corresponds to the collective R¹, R², and R³. 46. The method of any one of Paras. 33-45, wherein the chloride to —OR^(x) molar ratio is from 1 to 10.

Para. 47. The method of any one of Paras. 33-46, wherein the solid pre-catalyst system comprises Ti from 0.5 wt % to 30 wt %.

Para. 48. The method of any one of Paras. 33-47, wherein the solid pre-catalyst system comprises Mg from 1 wt % to 20 wt %.

Para. 49. The method of any one of Paras. 33-48, wherein the solid pre-catalyst system comprises Al from 1 wt % to 20 wt %.

Para. 50. The method of any one of Paras. 33-49, wherein the solid pre-catalyst system comprises pre-catalyst particles having a D₅₀ from 1 μm to 15 μm.

Para. 51. The method of any one of Paras. 33-50, wherein the solid pre-catalyst system is further contacted with a reducing agent.

Para. 52. The method of Para. 51, wherein the reducing agent comprises diethyl aluminum chloride (DEAC), triethyl aluminum (TEA), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), triisobutyl aluminum (TiBA), trimethyl aluminum (TMA), methylaluminoxane (MAO), or a mixture of any two or more thereof.

Para. 53. The method of any one of Paras. 33-52, wherein the solid catalyst system is configured to polymerize, or co-polymerize, an olefin monomer.

Para. 54. The method of any one of Paras. 33-53, wherein the olefin monomer comprises ethylene, propylene, 1-butene, 4-methyl-1-pentene, 1-hexene, 1-octene, or a mixture of any two or more thereof.

Para. 55. The method of any one of Paras. 33-54, wherein the solid catalyst system exhibits an olefinic polymerization catalyst efficiency (CE) of greater than 2 kg_(PE)·g_(Cat) ⁻¹·h⁻¹.

Para. 56. The method of any one of Paras. 33-55, wherein the olefin comprises ethylene, the method further comprises collecting polyethylene exhibiting an intrinsic viscosity of greater than 1.0 dl/g.

While certain embodiments have been illustrated and described, it should be understood that changes and modifications may be made therein in accordance with ordinary skill in the art without departing from the technology in its broader aspects as defined in the following claims.

The embodiments, illustratively described herein may suitably be practiced in the absence of any element or elements, limitation or limitations, not specifically disclosed herein. Thus, for example, the terms “comprising,” “including,” “containing,” etc. shall be read expansively and without limitation. Additionally, the terms and expressions employed herein have been used as terms of description and not of limitation, and there is no intention in the use of such terms and expressions of excluding any equivalents of the features shown and described or portions thereof, but it is recognized that various modifications are possible within the scope of the claimed technology. Additionally, the phrase “consisting essentially of” will be understood to include those elements specifically recited, and those additional elements that do not materially affect the basic and novel characteristics of the claimed technology. The phrase “consisting of” excludes any element not specified.

The present disclosure is not to be limited in terms of the particular embodiments described in this application. Many modifications and variations may be made without departing from its spirit and scope, as will be apparent to those skilled in the art. Functionally equivalent methods and compositions within the scope of the disclosure, in addition to those enumerated herein, will be apparent to those skilled in the art from the foregoing descriptions. Such modifications and variations are intended to fall within the scope of the appended claims. The present disclosure is to be limited only by the terms of the appended claims, along with the full scope of equivalents to which such claims are entitled. It is to be understood that this disclosure is not limited to particular methods, reagents, compounds, compositions, or biological systems, which can of course vary. It is also to be understood that the terminology used herein is for the purpose of describing particular embodiments only, and is not intended to be limiting.

In addition, where features or aspects of the disclosure are described in terms of Markush groups, those skilled in the art will recognize that the disclosure is also thereby described in terms of any individual member or subgroup of members of the Markush group.

As will be understood by one skilled in the art, for any and all purposes, particularly in terms of providing a written description, all ranges disclosed herein also encompass any and all possible subranges and combinations of subranges thereof. Any listed range may be easily recognized as sufficiently describing and enabling the same range being broken down into at least equal halves, thirds, quarters, fifths, tenths, etc. As a non-limiting example, each range discussed herein may be readily broken down into a lower third, middle third and upper third, etc. As will also be understood by one skilled in the art all language such as “up to,” “at least,” “greater than,” “less than,” and the like, include the number recited and refer to ranges which may be subsequently broken down into subranges as discussed above. Finally, as will be understood by one skilled in the art, a range includes each individual member.

All publications, patent applications, issued patents, and other documents referred to in this specification are herein incorporated by reference as if each individual publication, patent application, issued patent, or other document was specifically and individually indicated to be incorporated by reference in its entirety. Definitions that are contained in text incorporated by reference are excluded to the extent that they contradict definitions in this disclosure.

Other embodiments are set forth in the following claims. 

What is claimed is:
 1. A method of preparing a solid pre-catalyst system, the method comprising: in a reactor under agitation with a stirring mechanism, reacting a colloidal suspension of an organic solvent and a complex of Formula I with a halogenated compound or a mixture of halogenated compounds at a starting reactor temperature; allowing the colloidal suspension to react exothermically under a controlled feed rate to form a precipitate, which is then allowed to reach an upper temperature limit for a sufficient period of time to form a reacted colloidal suspension; and allowing the reacted colloidal suspension to cool to completion temperature; wherein: the complex of Formula I is: XTiCl_(p)(OR¹)_(4-p)·YMg(OR²)_(q)(OR³)_(t)  (I) a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; R² is not the same as R³; and the precipitate exhibits a D₅₀ from about 3 μm to about 10 μm.
 2. The method of claim 1, wherein the complex of Formula I exhibits Fourier transform infrared C—H stretching vibration bands at wavenumber from 2500 cm⁻¹ to 5000 cm⁻¹.
 3. The method of claim 1, wherein the starting reactor temperature is about −10° C. to about 60° C.
 4. The method of claim 1, wherein the upper temperature limit is less than about 70° C.
 5. The method of claim 4, wherein the upper temperature limit is about 60° C.
 6. The method of claim 1, wherein the completion temperature is about 35° C. to about 60° C. and the agitation comprises stirring the reacted colloidal suspension at about 400 rpm to 2000 rpm.
 7. The method of claim 1 further comprising collecting the precipitate and washing the precipitate with an organic solvent or a mixture of organic solvents comprising alkanes, aromatics, or a mixture of any two or more thereof.
 8. The method of claim 7, wherein organic solvent comprises n-hexane.
 9. The method of claim 1, wherein the halogenated compound or a mixture of halogenated compounds comprises diethyl aluminum chloride (DEAC), ethylaluminum sesquichloride (EASC), ethyl aluminum dichloride (EADC), titanium tetrachloride (TiCl₄), silicon tetrachloride (SiCl₄) or a mixture of any two or more thereof.
 10. The method of claim 1, wherein the reacting comprises charging the reactor with a first portion of the organic solvent and the halogenated compound or a mixture of halogenated compounds, and adding the complex of Formula I in a second portion of the solvent to the reactor at a first feed rate.
 11. The method of claim 10, wherein parameters of turbidity of a reaction medium k_(T) are from 1.5 to 4.0 h⁻¹ and a maximum turbidity unity (TU_(max)) relative to image analysis is from 0.4 to 1.0 TU.
 12. The method of claim 1, wherein the reacting comprises charging the reactor with a first portion of the organic solvent and the complex of Formula I, and adding the halogenated compound or a mixture of halogenated compounds in a second portion of the solvent to the reactor at a first feed rate.
 13. The method of claim 12, wherein the first feed rate is from 0.05 mL/min to about 4.0 mL/min.
 14. The method of claim 12, wherein the starting reactor temperature is about −10° C., the upper temperature limit is about 60° C., and the sufficient period of time is about 1 hour, and the completion temperature is about 40° C.
 15. A solid pre-catalyst system comprising solid particles of a reaction product of a complex of Formula I with a halogenated compound or a mixture of halogenated compounds; wherein: XTiCl_(p)(OR¹)_(4-p)·YMg(OR²)_(q)(OR³)_(t)  (I) a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; R² is not the same as R³; and the solid particles exhibit a D₅₀ from about 3 μm to about 12 μm.
 16. A method of polymerizing or co-polymerizing olefin monomers, the method comprising: contacting a solid pre-catalyst system comprising solid particles of a composite of a reaction product of a halogenated compound and a colloidal suspension of a complex of Formula I with a reducing agent, optionally a chain transfer agent, and the olefin monomers: XTiCl_(p)(OR¹)_(4-p)·YMg(OR²)_(q)(OR³)_(t)  (I) wherein: a molar ratio of X to Y (X/Y) is from 0.2 to 5.0; p is 0 or 1; 0<q<2; 0<t<2; the sum of q and t is 2; R¹, R², and R³ are each independently a linear or branched alkyl, a linear or branched heteroalkyl, a cycloalkyl, a substituted cycloalkyl, a substituted heterocycloalkyl, a substituted aryl, or a (heteroaryl)alkyl; R² is not the same as R³; and the solid particles exhibit a D₅₀ from about 3 μm to about 12 μm.
 17. The method of claim 16, wherein the olefin monomer is ethylene, and the method further comprises collecting polyethylene exhibiting number average molar mass (M_(n)) between 10-250 kg/mol, or a weight average molar mass (M_(w)) between 150-1250 kg/mol, and wherein the polyethylene exhibits a polydispersity (M_(w)/M_(n)) from 3 and
 8. 18. The method of claim 16, wherein the olefin monomer is ethylene, and the method further comprises collecting polyethylene, and wherein less than 5 wt % of the polyethylene is eluted with 1,2-dichlorobenzene below 30° C. by crystallization elution fractionation (CEF) analysis. 